CN103663589A - Seawater desalinization method and seawater desalinization device - Google Patents
Seawater desalinization method and seawater desalinization device Download PDFInfo
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- CN103663589A CN103663589A CN201310686162.0A CN201310686162A CN103663589A CN 103663589 A CN103663589 A CN 103663589A CN 201310686162 A CN201310686162 A CN 201310686162A CN 103663589 A CN103663589 A CN 103663589A
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- Y02A20/124—Water desalination
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 the following contention in world resource will be caused by water "; Scientist says " water is irreplaceable ", " water is can not do forever not complete science proposition "; 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 and water as it is, will produce a series of serious consequence; Once resource exhausts, expanding economy, the various ecosystem and human health and existence all will be on the hazard.Expectation is in 21st century, and water is to the mankind's importance by the same to the mankind's importance in 20th century with oil, and water will become a kind of scarce commodity that determines national wealth.Water industry is by the industry that is 21st century maximum.In tellurian gross amount of water resources, fresh water only accounts for 2. 5 %, and seawater has accounted for 97. 5 %, and in a sense, seawater is only inexhaustible, nexhaustible main water source.Therefore, development desalination technology, to ocean, wanting fresh water is to solve the most effective means of Freshwater resources imbalance between supply and demand.China is the extremely country of shortage of a water resources.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-water countries in the world.In Northern Coastal Provinces, be one of water-deficient area of China especially.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 of northern China (city) per capita comprehensive water-using amount will reach respectively 325～365 M
3with 350～400 M
3, lack of water total amount will reach respectively 166～25,500,000,000 M
3with 273～39,300,000,000 M
3; Meanwhile, consider the poor and resource water shortage status of the water quality of southern coastal some areas, the lack of water situation of coastland will be severeer.Sea water desaltination is to solve one of fundamental way of coastland water scarcity, the Freshwater resources bottleneck that has 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 evaporation method, electroosmose process, ion exchange method etc.All there is certain defect in these methods.The apparatus structure using is more complicated, and manufacturing cost is higher, and operation energy consumption is high.Main stream approach is at present: low-temperature multi-effect method, multistage flash evaporation method, these three kinds of methods of high pressure reverse osmosis method.According to the situation statistics in 2007 annual sea water desaltination markets, in Middle East, the share of market of multistage flash evaporation method (MSF) has surpassed 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 evaporation method (MSF) in three kinds of mainstream technologys or maximum.Multistage flash evaporation (MSF) also has the main technical characteristics of reverse osmosis method (RO) to be with low-temperature multi-effect (MED): multistage flash evaporation (MSF) current consumption 4. 0～5. 5 kWh/ tons, its scale and capacity are current maximum, also lower to raw material water quality requirement, fouling of heat exchangers is medium, operation top temperature is at 90～112 ℃, but equipment cost is higher.Low-temperature multi-effect method (MED) current consumption is 2. 5～3. 5kWh/ ton, 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 70 ℃ of left and right.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-purpose condenser is specifically designed to steam, and working efficiency is lower.Use more multistage flash evaporation method 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, and energy consumption is high, and vacuum persistent state is poor.At present, China's sea water desaltination cost is approximately 5 yuan/ton of left and right, far away higher than tap water cost.In the world today, extensive sea water desalinating plant adopts multistage flash evaporation method exactly, although this technology has used decompression to carry out technology, 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 the strong brine temperature of its discharge is also more than 43 ℃.And use at present more desalination technology, be high pressure reverse osmosis technology, 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 device and method that improves sea water desaltination efficiency with heat pump ", 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, overcomes the above-mentioned defect that prior art exists, and provides a kind of heat energy recycling rate high, and 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 its technical problem employing is:
The present invention's method for desalting seawater is:
Seawater, after interchanger, directly enters vaporizer, or flows through and be built-in with the fresh water circulating box of another interchanger, after the fresh water heat absorption in fresh water circulating box, enters vaporizer again, before and after the evaporation work of seawater in vaporizer divides, two sections complete: the leading portion evaporation work of seawater is, seawater mainly relies on the heat of self in vaporizer, to realize evaporation (when seawater is to flow through to be built-in with the fresh water circulating box of 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 absorbing from the fresh water place in fresh water circulating box), the back segment evaporation work of seawater: seawater absorbs the fresh water latent heat that vaporizer internal recycling and evaporates in the first vaporizer (is the latent heat of the fresh water that circulates during seawater absorbs fresh water circulation loop in the first vaporizer, described fresh water circulation loop consists 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, at condensation injector place, carry out condensation, steam is given fresh water Feedback of latent heating again at condensation injector place, fresh water temperature is raise, 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 injected recycle pump suction vaporizer again from fresh water circulating box, fresh water temperature after heat exchange reduces, fresh water after temperature reduces receives the steam feedback being produced by the evaporation of vaporizer maritime interior waters and the latent heat coming at condensation injector place, by condensation and evaporation mode, realize heat circulation and transfer, by condensation injector, in mass transfer process, also pass again thermal property and realize desalting process, the strong brine producing after the evaporation of vaporizer maritime interior waters is discharged by strong brine overboard pump, by condensation injector, be injected into the fresh water in fresh water circulating box, after cooling, collect.
Before fresh water enters condensation injector, temperature only has 25 degree left and right, like this, be conducive to improve the efficiency of injection and condensing water vapor, realize continually and inject heat to vaporizer, the fluid that injects heat support is exactly jetting fluid (being fresh water), and spray liquid flow body heat content itself is just from absorbed the latent heat that steam discharged of coming by injection.Evaporation of seawater is inhaled latent heat major part from the fresh water in working cycle, and the latent heat that fresh water heat energy discharges in condensation injector place from steam, because the mode of fresh water circulation must flow through vaporizer.Vaporizer is by forming this kind of countercurrent heat exchange method, and by condenser is set in vaporizer, the circulation fresh water that the fresh water that makes to enter vaporizer is comparatively high temps, and the fresh water that flows out vaporizer is the fresh water that temperature is lower.From the strong brine of vaporizer discharge, by strong brine overboard pump, can carry out again double evaporation-cooling and concentrate, evaporate and concentrate for three times, evaporate and concentrate for four times, even evaporating and concentrate for five times etc.
The present invention's sea water desalinating plant comprises the first spraying cycle pump, the first condensation injector, the first fresh water circulating box and the first vaporizer; The first fresh water circulating box bottom is connected with the inlet end of the first vaporizer by pipeline, the exit end of the first vaporizer is connected with the inlet end of the first spraying cycle pump by pipeline, the first spraying cycle pump outlet end is connected with the inlet end of the first condensation injector by pipeline, the exit end of the first condensation injector is provided with the mouth of pipe and stretches into the 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; The 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 with the inlet end of the second interchanger by pipeline, the exit end of the second interchanger is connected with the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box inside by pipeline, 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 the first vaporizer is connected by strong brine overboard pump of pipeline.
Further, described the 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 the second interchanger is connected with the first vaporizer is provided with the first valve.
Further, the exit end of described the second interchanger is provided with the second valve with the pipeline that the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box inside is connected.
Further, the pipeline that described the 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 with the inlet end of the 4th interchanger by pipeline, the exit end of the 4th interchanger is connected with the inlet end of the 5th interchanger in being placed in the second fresh water circulating box by pipeline, 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 the pipeline road in the second fresh water circulating box, the second fresh water circulating box bottom is connected with the inlet end of the second vaporizer by pipeline, the exit end of the second vaporizer is connected with the inlet end of the second condensation injector by the second spraying cycle pump, the second vaporizer is connected with secondary strong brine overboard pump by pipeline.
Further, described the second fresh water circulating box bottom is also connected with another inlet end of First Heat Exchanger by pipeline.
Further, the pipeline that described the second fresh water circulating box is connected with another inlet end of First Heat Exchanger is provided with the 4th valve.Described the 3rd valve is a fresh water output variable valve, and the 4th valve is secondary fresh water output variable valve.
Further, described the first vaporizer substitutes with the 3rd vaporizer that is built-in with condenser.
Further, the inlet end of the condenser in described the 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, condenser below in the 3rd vaporizer is provided with condensed water suction pump, the exit end of well heater is connected to the 3rd vaporizer by pipeline, the 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 the pipeline in the 3rd fresh water circulating box, the 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 the 3rd vaporizer and condenser are one-piece construction.
Further, described the 3rd vaporizer is by the external strong brine discharge line of another strong brine overboard pump.
Further, described the 3rd fresh water circulating box is by the external fresh water discharge line of check valve.
The present invention utilizes condensation injector to make the inner relative vacuum that forms of vaporizer, and the seawater that makes to enter in vaporizer carries out the evaporation of lesser temps under relative vacuum environment.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 occasions such as vacuum-drying.Condensation injector mainly contains following feature: 1. with multi-nozzle structure formation make water and vapour contact area large, be conducive to energy exchange, can make vapour fully 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, machinery-free 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. can replace Large Towers class, still class, oil-sealed rotary pump and condensing equipment.Yet, improve the working efficiency of condensation injector, because performance and the efficiency change of condensation injector are larger, it is both relevant with structural shape, size and the workmanship of complete assembly, also have much relations with working conditions.Need further investigation and grasp relevant rule, could realize high efficiency operation.The working efficiency of complete assembly not only depends on condensation injector design optimization degree, the size that also depends on each significant parameter point in this device workflow, as by the temperature of injection medium fluid temperature, injection fluid, spray in addition the flow velocity of fluid and the size of pressure etc.; The PLB2000 model parameter that Cong Hujiang ejector vacuum pump factory produces 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 ℃, work water temperature is 25 ℃, when in driven fluid volume, vacuum tightness is 660mmHg, this condensation injector suction secondary steam amount is 2000kg/h, and while being reduced to 200mmHg gradually along with vacuum tightness, its aspiration has increased to 20000kg/h, but in evaporation cavity, must maintaining 91 ℃ of above temperature, just can to make in evaporation cavity absolute pressure reach 560mmHg(vacuum tightness be 200mmHg), this just need to give in evaporation cavity the more heat energy of injection.The circulation pump power of being joined that model is PSB-500 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, can find out when vacuum tightness declines 73% left and right, its aspiration increase by 1000%.It should be pointed out that the condensation of chewing with single spraying is sprayed compares, although the condensation injector efficiency of high-order many nozzles is high, and under conventional higher vacuum tightness (as the i.e. 630～670mmhg of 84～89kpa), its efficiency or obviously reduce.Therefore, under high vacuum, with condensation injector, vacuumize and will consume larger power.The kind of condensation injector is a lot, mode of operation with have many uses generally, it is simple in structure, easy to manufacture, bookkeeping convenient.In fact, sea water desaltination is not need very high vacuum environment, in order to acquire fresh water, rather than the salt solution of seawater after concentrated, it is just enough that we only need that seawater is concentrated into 6% left and right.Condensation injector is also of great significance for sea water desaltination, this is based on comparing gained out with other various desalination technologies, even if vacuum tightness is reduced to below 14Kpa, can finely realize evaporation of seawater problem, by constantly injecting heat energy to seawater, realize, this heat energy can adopt Recycle design to realize.Reduce injection stream temperature and rising driven fluid temperature and can improve induction efficiency, but consider driven fluid is heated and will be consumed more heat energy, and reduce injection stream temperature, also will consume more electric energy, therefore do not calculate.Yet, the present invention is condensed into liquid state and discharges latent heat at condensation injector place spraying injection steam out, this part latent heat again feeds back to and sprays operating fresh water, make this part latent heat fully obtain recycle, and again this partial heat energy is sucked in vaporizer by spraying cycle pump, allow fresh water latent heat in Absorption by Sea Water circulation and evaporated, this part heat energy reduces again to seawater so, so the fresh water temperature flowing out from vaporizer becomes lower, like this, be conducive to improve the efficiency of 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, circulation again and again, and inject more heat need not to the seawater that flows into vaporizer, lower the temperature also need not to the fresh water that enters condensation injector, the low temperature fresh water for spraying that can obtain wanting, the vaporization heat that should possess in the time of also can obtaining evaporation of seawater simultaneously, thereby realize the circulation of most of heat energy, we only need disposable injection heat energy, in vaporizer, evaporate, condensation in injector, realize the working cycle that heat energy goes round and begins again.And the heat exchange of carrying out with condensation and evaporation mode can be saved the heat interchanging area of interchanger.Existing condensation injector, not by heat energy recycling, is just heated to required dry thing simply, or opposing jet body to carry out water cooling tower cooling, can be also 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, during sewage disposal, water constituent major part need to be evaporated, and so just can realize the zero release of sewage, makes most water in sewage obtain recycle.So cost of sewage disposal is higher than sea water desaltination cost, because concentration is higher, water-absorbent is just higher, and water evaporation difficulty just strengthens, and because concentration of wastewater is larger, stops up interchanger possibility just larger.
Device volume of the present invention is little, occupy little space, stable and reliable operation, without configuration suction air device, working efficiency is high, steam output is also large, to consume power source few, vacuum persistent 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 electricity/tons simultaneously, more energy-conservation; Proper scale preparing fresh not only, is also specially adapted to the places such as the western water quality of submarine, steamer, island and China is poor for producing the fresh water of drinking, 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, the first condensation injector 3, the first fresh water circulating box 4 and the first vaporizer 1; The first fresh water circulating box 4 bottoms are connected with the inlet end of the first vaporizer 1 by pipeline, the exit end of the first vaporizer 1 is connected with the inlet end of the first spraying cycle pump 2 by pipeline, the exit end of the first spraying cycle pump 2 is connected with the inlet end of the first condensation injector 3 by pipeline, the exit end of the first condensation injector 3 is provided with the mouth of pipe and stretches into the 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; The first fresh water circulating box 4 inside are 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 with the inlet end of the second interchanger 6 by pipeline, the exit end of the second interchanger 6 is connected with the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box 4 inside by pipeline, the inlet end of First Heat Exchanger 7 is that the exit end of seawater inflow end 9, the second interchanger 6 is also connected to the first vaporizer 1 by pipeline;
Described the first vaporizer 1 is connected by strong brine overboard pump of pipeline 5.
Described the first fresh water circulating box 4 bottoms are 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 the 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 the second interchanger 6 is connected with the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box 4 inside is provided with the second valve 11.
The pipeline that described the first fresh water circulating box 4 bottoms are connected with another inlet end of First Heat Exchanger 7 is provided with the 3rd valve 12.
Described the first spraying cycle pump 2, the first condensation injector 3, the first fresh water circulating box 4 and the first vaporizer 1 form fresh water circulation loop.
The present invention's efficient sea water desalting method: 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 again the second interchanger 6, the second interchanger 6 is mainly used in injecting heat into seawater, seawater has two current available through route after by the second interchanger 6: article one seawater route of flowing through is, when circulation fresh water excess Temperature, the first valve 10 is closed, the second valve 11 is opened, when seawater passes through the interchanger of the first fresh water circulating box 4 inside, fresh water in the first fresh water circulating box 4 passes to seawater by its most of heat, seawater relies on the heat of self and obtains heat from fresh water, enter the interior realization evaporation of the first vaporizer 1, seawater self temperature declines, complete thus the leading portion evaporation work of seawater, after seawater completes leading portion evaporation work, seawater absorbs the latent heat of the fresh water circulating in fresh water circulation loop in the first vaporizer, realizes extra large evaporation of water, completes thus the back segment evaporation work of seawater.Another seawater route of flowing through is, the first valve 10 is opened, the second valve 11 is closed, seawater directly enters the interior evaporation of the first vaporizer 1 by the first valve 10 and produces steam, now, seawater equally also divides two sections of front and back to complete (the leading portion evaporation work of seawater: seawater relies on the heat of self in the interior realization evaporation of 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 circulating in fresh water circulation loop in the first vaporizer, realizes extra large evaporation of water).The power that the first condensation injector 3 provides by the first spraying cycle pump 2, after the fresh water sucking-off in the first fresh water circulating box 4, while flowing through the first vaporizer 1, the heat energy of fresh water is converted into the required latent heat of evaporation of seawater (above in mention " seawater absorbs the latent heat of the fresh water circulating in fresh water circulation loop in the first vaporizer "), fresh water temperature reduced and squeeze in the first condensation injector 3 and carry out condensation injection, by the first condensation injector 3, being injected into the first fresh water circulating box 4; Meanwhile, the steam of the first vaporizer 1 inside is carried out condensation by injection to the first condensation injector 3, thereby makes steam latent heat feed back to again fresh water.The seawater being concentrated is discharged (now, also can this part strong brine will be evaporated again for the second time and concentrated, refer to embodiment 2) by the strong brine overboard pump 5 being connected with the first vaporizer 1.By the first condensation injector 3, be injected into the fresh water of the first fresh water circulating box 4, through the 3rd valve 12, flow to First Heat Exchanger 7, after by First Heat Exchanger 7, fresh water temperature being declined, by fresh water collecting end 8, flowed out, by peripheral equipment fresh water standby pool, collect.First Heat Exchanger 7 is when lowering the temperature to fresh water, and the heat of fresh water output can, for flowing into and hold 9 Absorption by Sea Water that flow into from seawater, be realized flow into the preliminary intensification of the seawater of end 9 inflows 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, strong brine overboard pump 5 output terminal are connected with circulating and evaporating concentration systems again.
The present embodiment take one again circulating and evaporating concentration systems describe as example.
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 with the inlet end of the 4th interchanger 18 by pipeline, the exit end of the 4th interchanger 18 is connected with the inlet end of the 5th interchanger in being placed in the second fresh water circulating box 16 by pipeline, 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 the pipeline in the second fresh water circulating box 16, the second fresh water circulating box 16 bottoms are connected with the inlet end of the second vaporizer 13 by pipeline, 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, the second vaporizer 13 is connected with secondary strong brine overboard pump 19 by pipeline.
Described the second fresh water circulating box 16 bottoms are connected with another inlet end of First Heat Exchanger 7 by pipeline.
The pipeline that described the 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 the 3rd valve 12 is a fresh water output variable valve, and the 4th valve 17 is secondary fresh water output variable valve.
After strong brine overboard pump 5 is squeezed into the concentrated seawater that evaporation is discharged for the first time the 4th interchanger 18 and is heated, in the second fresh water circulating box 16, carry out heat balance, and then in inflow the second vaporizer 13, evaporate for the second time and concentrate, vaporized steam enters in the second fresh water circulating box 16 after by the second condensation injector 15 injection condensations, most of fresh water flows out the second fresh water circulating box 16 and sucks the interior release latent heat of 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 and carry out work by the second spraying cycle pump 14, remove the steam in injection condensation the second vaporizer 13, like this, complete again and again working cycle, finally, by secondary strong brine overboard pump 19, the seawater again having concentrated is discharged or is pressed in the 3rd circulating and evaporating concentration systems.
Evaporation concentration concentration of seawater out generally can reach 6% left and right for the first time, for producing fresh water, generally adopt single vaporization with concentrated just enough, if need further highly enriched, user can arrange the concentration systems of circulating and evaporating again that a plurality of structures are identical 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, to provide outside the fresh water that respective spray recycle pump can use, can also play the effect of carrying out heat exchange with seawater, and each fresh water circulating box position is higher than corresponding evaporator, like this, in vaporizer, can not exist gas stifled, be convenient to spraying cycle pump yet and can not produce cavitation erosion situation.
Fresh water in described the first vaporizer 1, the second vaporizer 13 within it portion's loop direction must and seawater form adverse current, and seawater has evaporating space under the spray of corresponding evaporator top, evaporation a part of steam after and fallen warm seawater fall into can further obtain the latent heat of circulation fresh water and continue 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, thereby be conducive to improve the efficiency of 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 the first vaporizer substitutes with the 3rd vaporizer 28 that is built-in with condenser.
The present embodiment is by the interior condenser that arranges of 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 with the inlet end of well heater 30 by pipeline, condenser below in the 3rd vaporizer 28 is provided with condensed water suction pump 24, the exit end of well heater 30 is connected to the 3rd vaporizer 28 by pipeline, the 3rd vaporizer 28 is connected with the inlet end of recycle pump 20 by pipeline, 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 the pipeline in the 3rd fresh water circulating box 22, the 3rd fresh water circulating box 22 bottoms are 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.
The 3rd vaporizer 28 is by the external strong brine discharge line 26 of another strong brine overboard pump 25.
The 3rd fresh water circulating box 22 is by the external fresh water discharge line 27 of check valve 23.
What the present embodiment adopted is another kind of heat energy recycling mode, and by seawater, preheating in vaporizer realizes in the recycle of a part of heat energy.
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, guaranteeing in the enough situations of circulated heat, the seawater of follow-up inflow just need not inject so much heat, just make up the part heat energy losing in working cycle just passable, in fact, the heat energy that injects seawater is all transferred to the fresh water of circulation, and the fresh water heat of output carries out thermal exchange by the seawater with the whole device of firm inflow, fresh water temperature is lowered, just can flow into peripheral equipment fresh water standby pool.Evaporation is the mode the most efficiently of conducting heat with condensation, like this, not only can save many heat exchanger areas, reduce facility investment expense, can also accelerate heat circulation process, save energy, the dual function of performance condensation injector injection and condensing water vapor, evaporation of seawater steam out in corresponding condensation injector rapidly under condensation, meanwhile, the latent heat that condensation discharges constantly enters into again in the fresh water of working cycle, like this, for evaporation of seawater provides enough latent heat, allow heat energy obtain recycle again.Use the present invention, can not only guarantee the temperature that each vaporizer internal flow is enough, while making evaporation of seawater, there are enough vaporization heats, and can also guarantee that there is enough pressure (referring to that relative normal atmosphere is the absolute pressure under vacuum condition here) vaporizer inside, guarantee 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, the heat energy that just can avoid excessive seawater flow can slattern sea water circulating pump power and inject seawater, and sea water desaltination rate is to be advisable in 30% left and right, seawater flow is to be advisable in fresh water internal circulating load 75% left and right.
In prior art, condensation injector is only for being dried and aspirating steam, because its injection pressure (vaporizer in 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 when a lot, its efficiency is also with regard to corresponding reduction, and in injection process, can take away by the many heats of injection thing, so that temperature is too low, cause vacuum tightness too high, will be excessive and spray pressure reduction, like this, will strengthen injection flow velocity, and consume many powers of motor, only have to driven fluid and heat and just can make evaporator room pressure be brought up, and injection ratio is improved, but this will consume more multipotency undoubtedly.And the present invention is by heat energy recycling is got up, when vaporizer inner fluid temperature is guaranteed, make accordingly vacuum tightness lower, injection volume is guaranteed.
Device volume of the present invention is little, occupy little space, stable and reliable operation, without configuration suction air device, working efficiency is high, steam output is also large, to consume power source few, vacuum persistent 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 electricity/tons simultaneously; Proper scale preparing fresh not only, is also specially adapted to place such as the western water quality of submarine, steamer, island and China is poor and is used as and produces the fresh water of drinking, applied widely.
Claims (10)
1. a method for desalting seawater, is characterized in that, seawater, after interchanger, directly enters vaporizer, or flows through and be built-in with the fresh water circulating box of another interchanger, after the fresh water heat absorption in fresh water circulating box, enters vaporizer again, before and after the evaporation work of seawater in vaporizer divides, two sections complete: the leading portion evaporation work of seawater is that seawater mainly relies on the heat of self in vaporizer, to realize evaporation, when seawater is to flow through to be built-in with the fresh water circulating box of 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 absorbing from the fresh water place in fresh water circulating box, the back segment evaporation work of seawater: seawater absorbs the 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, at condensation injector place, carry out condensation, steam is given fresh water Feedback of latent heating again at condensation injector place, fresh water temperature is raise, 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 injected recycle pump suction vaporizer again from fresh water circulating box, fresh water temperature after heat exchange reduces, fresh water after temperature reduces is at condensation injector place, the steam that reception is produced by the evaporation of vaporizer maritime interior waters feeds back and next latent heat, by condensation and evaporation mode, realize heat circulation and transfer, by condensation injector, in mass transfer process, also pass again thermal property and realize desalting process, the strong brine producing after the evaporation of vaporizer maritime interior waters is discharged by strong brine overboard pump, by condensation injector, is injected into the fresh water in fresh water circulating box, after cooling, collects.
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; The first fresh water circulating box bottom is connected with the inlet end of the first vaporizer by pipeline, the exit end of the first vaporizer is connected with the inlet end of the first spraying cycle pump by pipeline, the first spraying cycle pump outlet end is connected with the inlet end of the first condensation injector by pipeline, the exit end of the first condensation injector is provided with the mouth of pipe and stretches into the 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; The 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 with the inlet end of the second interchanger by pipeline, the exit end of the second interchanger is connected with the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box inside by pipeline, 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 the first vaporizer is connected with a strong brine overboard pump by pipeline.
3. implement according to claim 2 the device of method for desalting seawater, it is characterized in that, described the 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 the device of implementing method for desalting seawater described in claim 2 or 3, it is characterized in that, the pipeline that the exit end of described the second interchanger is connected with the first vaporizer is provided with the first valve.
5. according to the device of implementing method for desalting seawater described in claim 2 or 3, it is characterized in that, the exit end of described the second interchanger is provided with the second valve with the pipeline that the inlet end that is placed in the 3rd interchanger of the first fresh water circulating box inside is connected.
6. implement according to claim 3 the device of method for desalting seawater, it is characterized in that, the pipeline that described the first fresh water circulating box bottom is connected with another inlet end of First Heat Exchanger is provided with the 3rd valve.
7. implement according to claim 2 the device of method for desalting seawater, 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 with the inlet end of the 4th interchanger by pipeline, the exit end of the 4th interchanger is connected with the inlet end of the 5th interchanger in being placed in the second fresh water circulating box by pipeline, 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 the pipeline in the second fresh water circulating box, the second fresh water circulating box bottom is connected with the inlet end of the second vaporizer by pipeline, the exit end of the second vaporizer is connected with the inlet end of the second condensation injector by the second spraying cycle pump, the second vaporizer is connected with secondary strong brine overboard pump by pipeline.
8. implement according to claim 7 the device of method for desalting seawater, it is characterized in that, described the second fresh water circulating box bottom is also connected with another inlet end of First Heat Exchanger by pipeline; The pipeline that described the second fresh water circulating box is connected with another inlet end of First Heat Exchanger is provided with the 4th valve.
9. implement according to claim 2 the device of method for desalting seawater, it is characterized in that, described the first vaporizer substitutes with the 3rd vaporizer that is built-in with condenser.
10. implement according to claim 9 the device of method for desalting seawater, it is characterized in that, described the 3rd vaporizer and condenser are one-piece construction.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110451711A (en) * | 2019-08-13 | 2019-11-15 | 武汉宏澳绿色能源工程有限责任公司 | A kind of system and method for realizing high-salt wastewater condensing crystallizing using air air lift |
| 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 |
| CN114014399A (en) * | 2021-11-06 | 2022-02-08 | 海南月壤科技控股有限公司 | Almost zero energy consumption seawater desalination method and system |
| CN115520935A (en) * | 2022-09-29 | 2022-12-27 | 中冶焦耐(大连)工程技术有限公司 | Method and system for recovering high-temperature condensed water of coking plant |
| CN117534155A (en) * | 2023-12-20 | 2024-02-09 | 江苏聚德环保科技有限公司 | Seawater desalination equipment and method with high desalination rate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3864215A (en) * | 1974-02-11 | 1975-02-04 | Alanson J Arnold | Method of Distilling Sea Water on Small Ships and Marine Platforms Having Internal Combustion Engine |
| CN101708871A (en) * | 2009-12-03 | 2010-05-19 | 招玉春 | Gradient preheating multistage evaporation-type seawater desalination power generation system |
| CN101948148A (en) * | 2010-10-22 | 2011-01-19 | 河北宏润重工集团有限公司 | Energy-saving low-temperature multiple-effect seawater desalting device |
| CN203582533U (en) * | 2013-12-16 | 2014-05-07 | 湖南创化低碳环保科技有限公司 | Sea water desalting device |
-
2013
- 2013-12-16 CN CN201310686162.0A patent/CN103663589B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3864215A (en) * | 1974-02-11 | 1975-02-04 | Alanson J Arnold | Method of Distilling Sea Water on Small Ships and Marine Platforms Having Internal Combustion Engine |
| CN101708871A (en) * | 2009-12-03 | 2010-05-19 | 招玉春 | Gradient preheating multistage evaporation-type seawater desalination power generation system |
| CN101948148A (en) * | 2010-10-22 | 2011-01-19 | 河北宏润重工集团有限公司 | Energy-saving low-temperature multiple-effect seawater desalting device |
| CN203582533U (en) * | 2013-12-16 | 2014-05-07 | 湖南创化低碳环保科技有限公司 | Sea water desalting device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110451711A (en) * | 2019-08-13 | 2019-11-15 | 武汉宏澳绿色能源工程有限责任公司 | A kind of system and method for realizing high-salt wastewater condensing crystallizing using air air lift |
| 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 |
| CN114014399A (en) * | 2021-11-06 | 2022-02-08 | 海南月壤科技控股有限公司 | Almost zero energy consumption seawater desalination method and system |
| CN115520935A (en) * | 2022-09-29 | 2022-12-27 | 中冶焦耐(大连)工程技术有限公司 | Method and system for recovering high-temperature condensed water of coking plant |
| CN117534155A (en) * | 2023-12-20 | 2024-02-09 | 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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