CN101734823A - Seawater desalination process with low cost - Google Patents
Seawater desalination process with low cost Download PDFInfo
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- CN101734823A CN101734823A CN200910264532A CN200910264532A CN101734823A CN 101734823 A CN101734823 A CN 101734823A CN 200910264532 A CN200910264532 A CN 200910264532A CN 200910264532 A CN200910264532 A CN 200910264532A CN 101734823 A CN101734823 A CN 101734823A
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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
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- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Abstract
The invention relates to a seawater desalination process with low cost, which utilizes the condensate of the vapor cycle of a thermal power plant or a nuclear power station as a heat source, heats seawater to the temperature of 60-80 DEG C and atomizes the seawater in an atomizing chamber. On the other hand, natural air is heated after being washed and humidified, enters the atomizing chamber and contacts the atomized high-temperature seawater mist flow so as to enable part of the atomized high-temperature seawater mist flow to be instantaneously vaporized; fresh water mist droplets generated by the atomization of the high-temperature seawater are lifted by the kinetic energy of air to move upwards; moreover, because the density of water is different from the density of salt, the water and the salt are separated in the movement process; the two blasts of fresh water airflow are cooled by the raw material of cold seawater simultaneously and condensed into fresh water, the heated raw material of the cold seawater is used for washing and humidifying the natural air, and clean air carrying water vapor is recycled after the clean air carrying the water vapor is cooled; and the entire process flow does not consume extra heat energy and only consumes the air and less electric energy required by the transportation of the seawater. The process recovers energy in the condensate of the vapor cycle of the thermal power plant or the nuclear power station, produces the fresh water in large amounts and also produces a by-product of concentrated seawater.
Description
Invention field
The present invention relates to desalination process.
Background technology
The world's two overall situation problems, the firstth, global warming, the secondth, water resources crisis.For article one, people have launched substantial action to reduce the discharging of greenhouse gases, reduce thermal pollution; For second, people have also recognized the seriousness of problem, and sayings such as " war of the following contention in world resource will be caused by water ", " after the energy dilemma, next crisis will take turns to the water crisis " are painted an alarming picture of the situation just to scare the audience by no means.Under these circumstances, desalination technology is subject to people's attention day by day, the emphasis that desalination technology especially less energy-consumption, that can reduce thermal pollution is researched and developed especially.At present, both at home and abroad proven technique is multistage flash evaporation method (MSF) and reverse osmosis method (RO), the market share of occupying the overwhelming majority, but these two kinds of method operation energy consumptions or production cost are all higher, because the MSF method also needs vacuum apparatus except that thermal source, and the RO rule needs pressure exerting device, all need consume a large amount of electric energy.
Because fossil energy is exhausted day by day, exploitation usage quantity for new forms of energy is more and more higher, such as nuclear energy, global Nuclear power plants quantity is more and more, similar with heat power plant, non-straight-line (straight-line be seawater directly circulate cooling) Nuclear power plants can produce a large amount of phlegma (about 70～80 ℃), and this part phlegma must just can recycle through after the cooling cooling.Therefore if can be, then be the energy but also can make environment exempt from the act of the doulbe-sides' victory of thermal pollution of not only having avoided waste with heat recovery and utilization wherein.
At above situation, the present invention proposes a kind of sea water desaltination novel process of utilizing the less energy-consumption of residual heat resources.
Summary of the invention
The purpose of this invention is to provide a kind of sea water desaltination novel process, this technology is applicable to the occasion of a large amount of residual heat resources, as heat power plant, Nuclear power plants etc.The low grade heat energy of recycling in water of condensation by this technology obtains fresh water (near deionized water) with low cost from seawater, make simultaneously to be sent back to steam generating system after the water of condensation cooling and to recycle.
Purpose of the present invention realizes by following technical process:
A kind of desalination process cheaply, as shown in Figure 1, it is made up of the following step:
Step 1. nature seawater enters pretreatment system S-01 by pipeline 1, utilize pretreatment unit to remove wherein organism and solid shape impurity such as sand grain, enter seawater basin V-01 by pipeline 2 then, after being sent by impeller pump I P-01, pipeline 3 is divided into two strands again, one stock-traders' know-how pipeline 6 enters interchanger I E-01, be delivered to washing conditioning tower T-01 top after being heated to 30～60 ℃, and its thermal source is a spray chamber T-02 top material; Another stock-traders' know-how pipeline 4 enters interchanger IV E-04, be warming up to 60～80 ℃ after pipeline 5 is delivered to spray chamber T-02 spraying, when this high temperature seawater is atomized, promptly produce a large amount of water smokes, because the dual function of air-flow and hot-fluid, salt are wherein separated the difference of density (mainly based on) in water smoke upward movement process with fresh water water smoke;
Step 2. natural air is by gas blower G-01, transport to through pipeline 8 and to enter washing conditioning tower T-01 bottom after interchanger II E-02 is heated to 35～55 ℃ again, in tower, rise, hot sea water counter current contact under with spraying from cat head, air is washed purification on the one hand in this process, humidification is on the other hand heated up, make vapour content wherein reach saturated under this operational condition, send into interchanger III E-03 through pipeline 10 then, the effusive seawater in washing conditioning tower T-01 bottom enters seawater basin V-01 through pipeline 12 and recycles.When operation operation, the concentration of seawater that pipeline 12 is discharged can be sent to concentrated seawater storage tank V-03 when bringing up to certain value, and the system halogen that is used to salt industry is produced or as the raw material of salt chemical engineering;
Step 3. enters T-02 by the effusive saturated moist air of interchanger III E-03 after continuing to be heated to 70～80 ℃, in uphill process, touch the high temperature seawater that in T-02, has been atomized, make the moisture content in the seawater partly be vaporizated into water vapor and rising, meanwhile, because the dual function of rising saturated moist air and hypogene water steam, make that the salt in the atomizing seawater is separated with fresh water water smoke, rise to the T-02 top and be mainly air by top duct 13 effusive fluids, water vapor and fresh water water smoke, and the liquid phase that descends in T-02 mainly is the higher concentrated seawater of saltiness, as long as the speed control of upstream is suitable among the T-02, only be air in the air-flow that can guarantee to rise, water vapor and fresh water water smoke;
Step 4. is through pipeline 13 effusive air, water vapor enters interchanger I E-01 with fresh water water smoke and is cooled to 5～30 ℃, heat-eliminating medium is the seawater that is local temperature, condensed fresh water enters fresh water receiving tank V-02 through pipeline 14, the Cryogenic air of not coagulating then is back to gas blower G-01 recycle through pipeline 21, the concentrated seawater (40～65 ℃) that spray chamber T-02 collects the bottom is then sent into the usefulness that washing conditioning tower T-01 cat head is made the spray humidification through pipeline 15 and impeller pump IIP-02, in addition, as long as regulate the flow proportional of pipeline 15 and pipeline 7, the concentration of the seawater that is concentrated with regard to may command washing conditioning tower T-01 bottom.
Step 5.70-80 ℃ of phlegma enters interchanger III E-03 through pipeline 18, enters interchanger II E-02 through pipeline 19 again after cooling is cooled to 40～60 ℃ and further is cooled to 5～35 ℃ and sends back to.
Above-mentioned desalination process cheaply, the thermal source of described interchanger IIIE-03 and interchanger IVE-04 can come from the steam condensate of heat power plant or nuclear power plant (about 70～80 ℃).
Can from seawater, produce fresh water continuously by above five steps, it is pointed out that above step there is no sequencing, under stable condition, four steps are carried out simultaneously, and organically combine, and this specification sheets just just is divided into four steps for convenience.
Above-mentioned low-cost desalination novel process has following some superior part:
One, desired raw material is nature seawater and natural air, for nature seawater, as long as the organism and the solid shape impurity such as sand grain that adopt pretreatment unit to remove wherein promptly can be used as the water source, and pretreatment unit suitable maturation and at present by widespread usage; Natural air then can be by direct drawing-in system behind the suitable filtration, purification as the carrier of moisture content and airflow kinetic energy;
Two, the energy consumption of system is mainly at interchanger E-03 and interchanger E-04, and their thermal source is the phlegma (about 70～80 ℃) of heat power plant or Nuclear power plants steam cycle, and itself just needs cooling process.Therefore this technology does not only need extra thermal source, and can alleviate the burden of cooling tower for heat power plant or Nuclear power plants, reduces the required electric power of cooling, and reduces the thermal pollution to environment;
Three, owing to water vapor in the natural air under the normal temperature does not reach capacity, therefore native system comes the humidification air with high temperature seawater earlier, make air fully absorb the fresh water in the seawater and reach water-vapo(u)r saturation, air themperature raises simultaneously, has further strengthened vapour content wherein again;
Temperature was 60～80 ℃ when four, high temperature seawater entered, and became tiny droplet through atomizing, made to conduct heat and the increase of isolating specific surface area.When contacting, droplet absorbs heat rapidly with pyritous wet air (70～80 ℃) when it, and part moisture content wherein is vaporized; Simultaneously, because the flow and the flow velocity of pyritous wet air are controlled in a certain proper range, the feasible fresh water droplet that is produced by the high temperature seawater atomizing is promoted by aerodynamic energy and moves upward, and owing to water separates in moving process with different being able to of density of salt, what the fresh water that comparable simple evaporation (comprising multistage) produces through the fresh water that obtains behind the cooling condensation will be big like this is many.
Five, the concentrated seawater that native system produced tentatively purifies, and water temperature and output are basicly stable throughout the year, and the system halogen that therefore can be directly used in salt industry is produced or as the raw material of development salt chemical engineering.
Description of drawings
Fig. 1 is the schematic flow sheet of specification sheets of the present invention and embodiment 1,2,3.Wherein:
S-01 is the sea water preprocessing device, V-01 is the seawater basin, V-02 is the fresh water holding tank, V-03 is the concentrated seawater storage tank, and P-01 and P-02 are impeller pump I and II, and E-01, E-02, E-03 and E-04 are interchanger I, II, III and IV, T-01 is the washing conditioning tower, T-02 is a spray chamber, and G-01 is a gas blower, and 1,2,3,4,5,6,7,8,9,10,11,12,13,14,15,16,17,18,19,20,21,22 is pipeline.
Embodiment
Below further specify the present invention by embodiment:
Embodiment 1: produce 20000 tons of pure water (summer) per year
Production equipment wherein washs 1.2 meters of conditioning tower T-01 diameters as shown in Figure 1, and is high 10 meters, and 1.6 meters of spray chamber T-02 diameters are high 6 meters; Behind impeller pump I P-01, be divided into two strands with 38 tons/hour flow through pretreated 25 ℃ of seawater, one enters washing conditioning tower T-01 top spray with 31 tons/hour flow after interchanger I E-01 heat exchange to 50 ℃, another strand enters the T-02 atomizing with 7 tons/hour flow after interchanger IVE-04 heat exchange to 75 ℃; 32 ℃ of natural airs through gas blower G-01 with 10000m
3The flow of/hr enters washing conditioning tower T-01 bottom after interchanger II E-02 is heated to 48 ℃, enter spray chamber T-02 after being heated to 78 ℃ once more by interchanger III E-03 behind the intensification humidification, be delivered to interchanger I E-01 by spray chamber T-02 top after making seawater vaporization part and carrying a large amount of fresh water droplets secretly and be cooled to 27 ℃, the fresh water that obtains 2.82 tons/hour enters fresh water holding tank V-02, does not coagulate air admission gas blower G-01 and recycles; 54 ℃ the concentrated seawater that spray chamber T-02 collects the bottom is then sent into washing conditioning tower T-01 cat head work spray through impeller pump II P-02 and is used.Interchanger IIIE-03 and interchanger IVE-04 consume 80 ℃ 10.8 tons/hour of hot water altogether.
Embodiment 2: produce 10000 tons of pure water (winter) per year
Production equipment wherein washs 0.9 meter of conditioning tower T-01 diameter as shown in Figure 1, and is high 8 meters, and 1.2 meters of spray chamber T-02 diameters are high 5 meters; Behind impeller pump I P-01, be divided into two strands with 18 tons/hour flow through pretreated 5 ℃ of seawater, one enters washing conditioning tower T-01 top spray with 14 tons/hour flow after interchanger I E-01 heat exchange to 46 ℃, another strand enters spray chamber T-02 atomizing with 4 tons/hour flow after interchanger IV E-04 heat exchange to 70 ℃; 5 ℃ of natural airs through gas blower G-01 with 6000m
3The flow of/hr enters washing conditioning tower T-01 bottom after interchanger II E-02 is heated to 39 ℃, enter spray chamber T-02 after being heated to 74 ℃ once more by interchanger III E-03 behind the intensification humidification, be delivered to interchanger I E-01 by spray chamber T-02 top after making seawater vaporization part and carrying a large amount of fresh water droplets secretly and be cooled to 6 ℃, the fresh water that obtains 1.36 tons/hour enters fresh water holding tank V-02, does not coagulate air admission gas blower G-01 and recycles; 49 ℃ the concentrated seawater that T-02 collects the bottom is then sent into washing conditioning tower T-01 cat head work spray and is used.Interchanger IIIE-03 and interchanger IVE-04 consume 75 ℃ 6.2 tons/hour of hot water altogether.
Embodiment 3: produce 20000 tons of pure water (winter) per year
Production equipment wherein washs 1.2 meters of conditioning tower T-01 diameters as shown in Figure 1, and is high 10 meters, and 1.6 meters of spray chamber T-02 diameters are high 6 meters; Behind impeller pump I P-01, be divided into two strands with 38 tons/hour flow through pretreated 5 ℃ of seawater, one enters washing conditioning tower T-01 top spray with 31 tons/hour flow after interchanger I E-01 heat exchange to 46 ℃, another strand enters spray chamber T-02 atomizing with 7 tons/hour flow after interchanger IV E-04 heat exchange to 70 ℃; 5 ℃ of natural airs through gas blower G-01 with 12000m
3The flow of/hr enters washing conditioning tower T-01 bottom after interchanger II E-02 is heated to 39 ℃, enter spray chamber T-02 after being heated to 75 ℃ once more by interchanger III E-03 behind the intensification humidification, be delivered to interchanger I E-01 by the T-02 top after making seawater vaporization part and carrying a large amount of fresh water drops secretly and be cooled to 6 ℃, the fresh water that obtains 2.75 tons/hour enters fresh water holding tank V-02, does not coagulate air admission gas blower G-01 and recycles; 49 ℃ the concentrated seawater that T-02 collects the bottom is then sent into washing conditioning tower T-01 cat head work spray and is used.Interchanger IIIE-03 and interchanger IV E-04 consume altogether 75 ℃ hot water 13..5 ton/hour.
Claims (2)
1. desalination process cheaply is characterized in that it is made up of the following step:
Step 1. nature seawater enters pretreatment system S-01 by pipeline 1, utilize pretreatment unit to remove wherein organism and solid shape impurity such as sand grain, enter seawater basin V-01 by pipeline 2 then, after being sent by impeller pump I P-01, pipeline 3 is divided into two strands again, one stock-traders' know-how pipeline 6 enters interchanger I E-01, be delivered to washing conditioning tower T-01 top after being heated to 30～60 ℃, and its thermal source is a spray chamber T-02 top material; Another stock-traders' know-how pipeline 4 enters interchanger IV E-04, be warming up to 60～80 ℃ after pipeline 5 is delivered to spray chamber T-02 spraying, when this high temperature seawater is atomized, promptly produce a large amount of water smokes, because the dual function of air-flow and hot-fluid, salt is wherein separated in water smoke upward movement process with fresh water water smoke;
Step 2. natural air is by gas blower G-01, transport to through pipeline 8 and to enter washing conditioning tower T-01 bottom after interchanger II E-02 is heated to 35～55 ℃ again, in tower, rise, hot sea water counter current contact under with spraying from cat head, air is washed purification on the one hand in this process, humidification is on the other hand heated up, make vapour content wherein reach saturated under this operational condition, send into interchanger III E-03 through pipeline 10 then, the effusive seawater in washing conditioning tower T-01 bottom enters seawater basin V-01 through pipeline 12 and recycles, when the operation operation, the concentration of seawater that pipeline 12 is discharged is sent to concentrated seawater storage tank V-03 when bringing up to designated value, and the system halogen that is used to salt industry is produced or as the raw material of salt chemical engineering;
Step 3. enters T-02 by the effusive saturated moist air of interchanger III E-03 after continuing to be heated to 70～80 ℃, in uphill process, touch the high temperature seawater that in T-02, has been atomized, make the moisture content in the seawater partly be vaporizated into water vapor and rising, meanwhile, because the dual function of rising saturated moist air and hypogene water steam, make that the salt in the atomizing seawater is separated with fresh water water smoke, rise to the T-02 top and be mainly air by top duct 13 effusive fluids, water vapor and fresh water water smoke, and the liquid phase that descends in T-02 mainly is the higher concentrated seawater of saltiness;
Step 4. is through pipeline 13 effusive air, water vapor enters interchanger I E-01 with fresh water water smoke and is cooled to 5～30 ℃, heat-eliminating medium is the seawater that is local temperature, condensed fresh water enters fresh water receiving tank V-02 through pipeline 14, the Cryogenic air of not coagulating then is back to gas blower G-01 recycle through pipeline 21,40～65 ℃ the concentrated seawater that spray chamber T-02 collects the bottom is then sent into the usefulness that washing conditioning tower T-01 cat head is made the spray humidification through pipeline 15 and impeller pump II P-02, in addition, as long as regulate the flow proportional of pipeline 15 and pipeline 7, the concentration of the seawater that is concentrated with regard to may command washing conditioning tower T-01 bottom;
Step 5.70-80 ℃ of phlegma enters interchanger III E-03 through pipeline 18, enters interchanger II E-02 through pipeline 19 again after cooling is cooled to 40～60 ℃ and further is cooled to 5～35 ℃ and sends back to.
2. desalination process cheaply according to claim 1 is characterized in that the thermal source of described interchanger IIIE-03 and interchanger IV E-04 can come from the steam condensate of heat power plant or nuclear power plant.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101973598A (en) * | 2010-10-15 | 2011-02-16 | 上海交通大学 | Spray evaporating air-moistening de-humidity type solar sea water desalinating device |
| CN102557176A (en) * | 2012-02-07 | 2012-07-11 | 绍兴文理学院 | Sea water desalinating device of cooling tower of coastal and island thermal power plants |
| CN102797523A (en) * | 2012-08-16 | 2012-11-28 | 中国核电工程有限公司 | Bleeder steam and exhaust steam comprehensive utilization method for nuclear turbine |
| CN103351034A (en) * | 2013-07-25 | 2013-10-16 | 江苏中核华纬工程设计研究有限公司 | High-temperature gas cooled reactor and low-temperature multiple-effect distillation seawater desalinization coupling device |
| CN103626243A (en) * | 2013-11-29 | 2014-03-12 | 福建省农业科学院农业生态研究所 | Extraction method and water solution phase-change separation system of purified water |
| CN103848464A (en) * | 2014-02-28 | 2014-06-11 | 长沙威保特环保科技有限公司 | Treatment method of low-temperature evaporation high-concentration sewage |
| CN106704115A (en) * | 2017-01-04 | 2017-05-24 | 国网辽宁省电力有限公司本溪供电公司 | Wind power cooling antifreezing system based on seawater source heat pump for wind power farm |
| CN106855030A (en) * | 2017-01-04 | 2017-06-16 | 国网辽宁省电力有限公司本溪供电公司 | The wind-powered electricity generation based on sea water source heat pump of wind power plant cools down antifreeze method |
| CN110759405A (en) * | 2019-11-06 | 2020-02-07 | 山东大学 | Waste heat utilization process and system for seawater direct-flow cooling water of power plant |
| CN111484092A (en) * | 2020-04-20 | 2020-08-04 | 山东省科学院能源研究所 | Contact heat exchange type sewage concentration system and process |
| CN112047412A (en) * | 2020-09-27 | 2020-12-08 | 长沙紫宸科技开发有限公司 | Seawater atomization cyclone desalination equipment system and method |
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2009
- 2009-12-25 CN CN2009102645325A patent/CN101734823B/en active Active
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101973598A (en) * | 2010-10-15 | 2011-02-16 | 上海交通大学 | Spray evaporating air-moistening de-humidity type solar sea water desalinating device |
| CN102557176B (en) * | 2012-02-07 | 2013-10-30 | 绍兴文理学院 | Sea water desalinating device of cooling tower of coastal and island thermal power plants |
| CN102557176A (en) * | 2012-02-07 | 2012-07-11 | 绍兴文理学院 | Sea water desalinating device of cooling tower of coastal and island thermal power plants |
| CN102797523A (en) * | 2012-08-16 | 2012-11-28 | 中国核电工程有限公司 | Bleeder steam and exhaust steam comprehensive utilization method for nuclear turbine |
| CN103351034B (en) * | 2013-07-25 | 2015-03-25 | 江苏中核华纬工程设计研究有限公司 | High-temperature gas cooled reactor and low-temperature multiple-effect distillation seawater desalinization coupling device |
| CN103351034A (en) * | 2013-07-25 | 2013-10-16 | 江苏中核华纬工程设计研究有限公司 | High-temperature gas cooled reactor and low-temperature multiple-effect distillation seawater desalinization coupling device |
| CN103626243A (en) * | 2013-11-29 | 2014-03-12 | 福建省农业科学院农业生态研究所 | Extraction method and water solution phase-change separation system of purified water |
| CN103626243B (en) * | 2013-11-29 | 2015-03-18 | 福建省农业科学院农业生态研究所 | Extraction method and water solution phase-change separation system of purified water |
| CN103848464A (en) * | 2014-02-28 | 2014-06-11 | 长沙威保特环保科技有限公司 | Treatment method of low-temperature evaporation high-concentration sewage |
| CN103848464B (en) * | 2014-02-28 | 2015-12-30 | 长沙威保特环保科技有限公司 | The treatment process of low-temperature evaporation high-concentration sewage |
| CN106704115A (en) * | 2017-01-04 | 2017-05-24 | 国网辽宁省电力有限公司本溪供电公司 | Wind power cooling antifreezing system based on seawater source heat pump for wind power farm |
| CN106855030A (en) * | 2017-01-04 | 2017-06-16 | 国网辽宁省电力有限公司本溪供电公司 | The wind-powered electricity generation based on sea water source heat pump of wind power plant cools down antifreeze method |
| CN106704115B (en) * | 2017-01-04 | 2019-04-05 | 国网辽宁省电力有限公司本溪供电公司 | The cooling winterization system of the wind-powered electricity generation based on sea water source heat pump of wind power plant |
| CN110759405A (en) * | 2019-11-06 | 2020-02-07 | 山东大学 | Waste heat utilization process and system for seawater direct-flow cooling water of power plant |
| CN111484092A (en) * | 2020-04-20 | 2020-08-04 | 山东省科学院能源研究所 | Contact heat exchange type sewage concentration system and process |
| CN112047412A (en) * | 2020-09-27 | 2020-12-08 | 长沙紫宸科技开发有限公司 | Seawater atomization cyclone desalination equipment system and method |
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