CN103508603B - Hot-membrane co-production sea water desalination method - Google Patents
Hot-membrane co-production sea water desalination method Download PDFInfo
- Publication number
- CN103508603B CN103508603B CN201310420656.4A CN201310420656A CN103508603B CN 103508603 B CN103508603 B CN 103508603B CN 201310420656 A CN201310420656 A CN 201310420656A CN 103508603 B CN103508603 B CN 103508603B
- Authority
- CN
- China
- Prior art keywords
- sea water
- water
- seawater
- desalination
- power plant
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
- Y02A20/131—Reverse-osmosis
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a hot-membrane co-production sea water desalination method which comprises an electric power plant sea water cooling system, an electric power plant sea water desulfurization system, an electric power plant smoke waste heat system and a sea water desalination system. Electric power plant flue gas waste heat is used for preheating sea water; the sea water enters the desalination system for desalination; the desalination system adopts a hot desalination system and a membrane desalination system which are in parallel; the defect that a hot method or a membrane method is used independently is overcome; waste gas waste heat is made full use of; water requirements in different regions and seasons are met; the fresh water cost is lowered; the thermal pollution to an environment is reduced; the salinity of the concentrated sea water after the desalination is 3.5-4%; the salt yield is increased by above 30% in comparison with common sea water; and the bromine production cost is lowered by approximately 50% in comparison with the common sea water.
Description
Technical field
The invention belongs to field of sea water desalting technology, be specifically related to a kind of method of hotting mask co-production sea water desalination, the mode that instant heating method and embrane method combine, meets different water demand, reduces fresh water cost.
Background technology
Water is Source of life, is the lifeblood of socio-economic development, is mankind's preciousness, irreplaceable natural resources.According to statistics, China's Freshwater resources total amount hundred million m more than 28000
3, occupy the 6th, the world, but occupancy volume per person only has 2200 m
3, be only 1/4 of world average level.The situation of current China Proposals of Water Resources is very severe, and the problems such as shortage of water resources, water pollutions are serious, water ecological environment deterioration become increasingly conspicuous, and have become the Main Bottleneck of the restriction sustainable development of socio-economy.
Sea water desaltination is the new and high technology that the world today is competitively studied, solve Freshwater resources effective way in short supply, method for desalting seawater in the market mainly contains Re Fa and embrane method, wherein hot method is evaporated by heating of seawater, vapor condensation is made to obtain the process of fresh water again, simple to operate, but cost is high, and energy consumption is large.Embrane method mainly reverse osmosis (RO) technology, reverse osmosis method is usually also known as ultra-filtration method, it utilizes semi-permeable membranes, allow under stress water through and salinity and impurity are retained, although reverse osmosis method method of specific heat in energy consumption is low by 10% ~ 20%, because membrane resistance is large, need by high-pressure pump in operation, and film is expensive, the life-span is short, has the decay of 50% every year; Secondly reverse osmosis method is relevant with the water quality of seawater, and whether water quality meets the requirements, and directly has influence on the work-ing life of permeable membrane; Meanwhile, reverse osmosis method requires higher to sea water preprocessing, seawater region, water temperature change in season.
In a word, high cost is the important factor of the domestic sea water desaltination development of at present restriction, is also that desalination water cannot the major reason of large-scale promotion.How two kinds of methods combining being got up respectively to get the chief to overcome two kinds of methods shortcoming separately, comprehensively its advantage, and made full use of by the concentrated seawater after desalination, is the problem that the present invention needs to solve.
Summary of the invention
Object of the present invention is exactly defect for above-mentioned existence and provides a kind of method of hotting mask co-production sea water desalination.This process costs is low, overcome the deficiency that Re Fa and embrane method are used alone existence, take full advantage of waste gas residual heat, meet the water demand in different geographical, season, reduce fresh water cost, decrease environmental thermal pollution, for coastland, particularly the city of shortage of fresh water has more important application value.
The method and technology scheme of a kind of hotting mask co-production sea water desalination of the present invention is, comprise power plant's salt water cooling system, power plant's Deuslfurizing system for sea water, and seawater desalination system, use the pre-hot sea water of power plant flue gas waste heat, then enter desalination system to desalinate, desalination system adopts hot method desalination system and embrane method desalination system in parallel, through the concentrated seawater of desalination system by carrying bromine device and enter salt making system and chlor-alkali devices preparing salt, chlorine and caustic soda.
Idiographic flow is:
1. seawater is drawn into power plant's salt water cooling system by sea-water pump, and seawater divides three routes to process afterwards;
2. Article 1 route, seawater enters power plant's Deuslfurizing system for sea water, and power plant's Deuslfurizing system for sea water is connected with power-plant flue gas bootstrap system, enters power plant's Deuslfurizing system for sea water after the flue gas in power-plant flue gas bootstrap system and seawater to make heat exchange;
3. Article 2 route, seawater enters power-plant flue gas bootstrap system, carry out countercurrent flow at this seawater and the flue gas of 140-150 DEG C come from boiler of power plant, enter Deuslfurizing system for sea water, the seawater after intensification enters low-temperature multi-effect desalting equipment and/or multistage flash evaporation desalting equipment is desalinated;
4. Article 3 route, embrane method desalination system: seawater enters sea-water reverse osmose apparatus;
5. step 2.-4. in concentrated seawater enter salt making system and carry out salt manufacturing and chlor-alkali devices by carrying bromine device and produce chlorine and caustic soda, fresh water enters pure water after-treatment system, is used as tap water or boiler feedwater after treatment.
Step 1. in seawater reach 24-35 DEG C through power plant's salt water cooling system temperature.
Step 3. at power-plant flue gas residual heat system, the flue-gas temperature after heat exchange reaches 100-110 DEG C, and the seawater temperature after heat exchange reaches 60-80 DEG C.
Step 4. middle sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment.
Pretreatment unit comprises that water conservancy diversion is micro-revolves reaction tank, inclined-plate clarifying basin, V-type sand-bed filter, clean water basin, R/O topping-up pump, high efficiency filter and cartridge filter; Desalting equipment comprises high pressure water pump and film desalting equipment.
Seawater enters that water conservancy diversion is micro-revolves reaction tank, and carry out flocculation reaction, the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, is 0.1-0.5m/s to flow velocity during outlet.
Inclined-plate clarifying basin swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
V-type sand filter fills effective size of grain 0.9-1.0mm quartz sand filtrate, and filter tank total inflow is 4000-5000m
3/ h, filtering velocity 7.0-8.0m/h.
R/O topping-up pump total flux 3500-4500 m
3/ h; High efficiency filter diameter 2000-4000mm, flow velocity 35-40m/h; Cartridge filter is PP filter core cartridge filter, filtering accuracy 4-6 μm.
Preferably, seawater enters that water conservancy diversion is micro-revolves reaction tank, and carry out flocculation reaction, the reaction times is 25 minutes, and inlet velocity is 0.5m/s, reduces gradually, is 0.2m/s to flow velocity during outlet.Inclined-plate clarifying basin swash plate length 1 m, settling tank upflow velocity 1.5mm/s; V-type sand filter fills effective size of grain 0.95mm quartz sand filtrate, and filter tank total inflow is 4600m
3/ h, filtering velocity 7.5m/h; R/O topping-up pump total flux 4200 m
3/ h; High efficiency filter diameter 3000mm, flow velocity 37.2m/h; PP filter core cartridge filter, filtering accuracy 5 μm.
Beneficial effect of the present invention is: the method cost of a kind of hotting mask co-production sea water desalination of the present invention is low, overcome the deficiency that Re Fa and embrane method are used alone existence, take full advantage of waste gas residual heat, meet the water demand in different geographical, season, reduce fresh water cost, decrease environmental thermal pollution, the concentrated seawater salinity after desalination is 3.5-4%, salt output can improve more than 30% than ordinary sea water, produces bromine and reduces about about 50% than ordinary sea water cost.
The method characteristic of a kind of hotting mask co-production sea water desalination of the present invention:
1, less investment: investment cost is the 1/2-2/3 of other techniques;
2, energy consumption is low: lower than other techniques by more than 20%;
3, to seawater strong adaptability, equipment mobility is strong.
The method economic target of a kind of hotting mask co-production sea water desalination of the present invention:
1, ratio of desalinization 99.7%;
2, Water Sproading rate 42%;
3, ton water power consumption 4-5 degree, and the about 6-7 degree of prior art ton water power consumption;
4, ton water running cost 4.5-5.5 unit, current hot method running cost is merely at about 7 yuan, and simple reverse osmosis method running cost is at about 5 yuan.
accompanying drawing illustrates:
Figure 1 shows that process flow diagram of the present invention.
In figure, 1. sea-water pump, 2. power plant's salt water cooling system, 3. Deuslfurizing system for sea water, 4. smoke waste heat utilization system, 5. boiler of power plant, 6. low-temperature multi-effect desalting equipment, 7. multistage flash evaporation desalting equipment, 8. water conservancy diversion is micro-revolves reaction tank, 9. inclined-plate clarifying basin, 10.V type sand filter, 11. clean water basin, 12.R/O topping-up pump, 13. high efficiency filters, 14. cartridge filters, 15. high pressure water pumps, 16. film desalting equipments, 17. pure water after-treatment systems, 18. boiler make up systems, 19. carry bromine device, 20. salt making systems, 21. chlor-alkali devices.
embodiment:
In order to understand the present invention better, describe technical scheme of the present invention in detail with specific examples below, but the present invention is not limited thereto.
The method of a kind of hotting mask co-production sea water desalination of the present invention, comprise power plant's salt water cooling system 2, power plant's Deuslfurizing system for sea water 3, and seawater desalination system, use the pre-hot sea water of power plant flue gas waste heat, then enter desalination system to desalinate, desalination system adopts hot method desalination system and embrane method desalination system in parallel, through the concentrated seawater of desalination system by carrying bromine device 19 and enter salt making system and chlor-alkali devices preparing salt, chlorine and caustic soda.
embodiment 1
Hot method is produced
1. seawater is drawn into power plant's salt water cooling system 2 by sea-water pump 1, and seawater reaches 24-35 DEG C through power plant's salt water cooling system 2 temperature, and seawater processes through following route afterwards;
2. Article 1 route, seawater enters power plant's Deuslfurizing system for sea water 3, and power plant's Deuslfurizing system for sea water 3 is connected with power-plant flue gas bootstrap system 4, enters power plant's Deuslfurizing system for sea water 3 after the flue gas in power-plant flue gas bootstrap system 4 and seawater to make heat exchange;
3. Article 2 route, seawater enters power-plant flue gas bootstrap system 4, countercurrent flow is carried out at this seawater and the flue gas of 140-150 DEG C come from boiler of power plant, flue-gas temperature after heat exchange reaches 100-110 DEG C, seawater temperature after heat exchange reaches 60-80 DEG C, enter Deuslfurizing system for sea water 3, the seawater after intensification enters low-temperature multi-effect desalting equipment 6 and/or multistage flash evaporation desalting equipment 7 is desalinated;
4. step 2., 3. in concentrated seawater enter salt making system 20 carry out salt manufacturing and chlor-alkali devices 21 produces chlorine and caustic soda by carrying bromine device 19, fresh water enters pure water after-treatment system 17, is used as tap water or boiler feedwater after treatment.
Table 1 is depicted as the parameter and energy consumption condition that described in embodiment 1, hot method is produced.
Table 1
。
embodiment 2
Embrane method is produced
1. seawater is drawn into power plant's salt water cooling system 2 by sea-water pump 1, and seawater reaches 24-35 DEG C through power plant's salt water cooling system 2 temperature;
2. embrane method desalination system: seawater enters sea-water reverse osmose apparatus, sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment; Pretreatment unit comprises that water conservancy diversion is micro-revolves reaction tank 8, inclined-plate clarifying basin 9, V-type sand-bed filter 10, clean water basin 11, R/O topping-up pump 12, high efficiency filter 13 and cartridge filter 14; Desalting equipment comprises high pressure water pump 15, energy recycle device and boost in pressure system and film desalting equipment 16.
Seawater enters that water conservancy diversion is micro-revolves reaction tank 8, and carry out flocculation reaction, the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, is 0.1-0.5m/s to flow velocity during outlet.
Inclined-plate clarifying basin 9 swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
V-type sand filter 10 fills effective size of grain 0.90-1.0mm quartz sand filtrate, filter tank total inflow 4000-5000m
3/ h, filtering velocity 7.0-8.0m/h.
R/O topping-up pump 12 total flux 3500-4500 m
3/ h; High efficiency filter 13 diameter 2000-4000mm, flow velocity 35-40m/h; Cartridge filter 14 is PP filter core cartridge filter, filtering accuracy 4-6 μm.
3. step 2. in concentrated seawater enter salt making system 20 carry out salt manufacturing and chlor-alkali devices 21 produces chlorine and caustic soda by carrying bromine device 19, fresh water enters pure water after-treatment system 17, is used as tap water or boiler feedwater after treatment.
Table 2 is depicted as the parameter that embrane method described in embodiment 2 is produced.
Table 2
。
Table 3 is depicted as power consumption and the relevant volume situation of embrane method production described in embodiment 2.
Table 3
。
embodiment 3
Hotting mask coproduction
Seawater is drawn into power plant's salt water cooling system 2 by sea-water pump 1, and seawater reaches 24-35 DEG C through power plant's salt water cooling system 2 temperature, and seawater processes through following route simultaneously afterwards; ;
2. Article 1 route, seawater enters power plant's Deuslfurizing system for sea water 3, and power plant's Deuslfurizing system for sea water 3 is connected with power-plant flue gas bootstrap system 4, enters power plant's Deuslfurizing system for sea water 3 after the flue gas in power-plant flue gas bootstrap system 4 and seawater to make heat exchange;
3. Article 2 route, seawater enters power-plant flue gas bootstrap system 4, countercurrent flow is carried out at this seawater and the flue gas of 140-150 DEG C come from boiler of power plant, flue-gas temperature after heat exchange reaches 100-110 DEG C, seawater temperature after heat exchange reaches 60-80 DEG C, enter Deuslfurizing system for sea water 3, the seawater after intensification enters low-temperature multi-effect desalting equipment 6 and/or multistage flash evaporation desalting equipment 7 is desalinated;
4. Article 3 route, embrane method desalination system: seawater enters sea-water reverse osmose apparatus, sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment; Pretreatment unit comprises that water conservancy diversion is micro-revolves reaction tank 8, inclined-plate clarifying basin 9, V-type sand-bed filter 10, clean water basin 11, R/O topping-up pump 12, high efficiency filter 13 and cartridge filter 14; Desalting equipment comprises high pressure water pump 15, energy recycle device and boost in pressure system and film desalting equipment 16.
Seawater enters that water conservancy diversion is micro-revolves reaction tank 8, and carry out flocculation reaction, the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, is 0.1-0.5m/s to flow velocity during outlet.
Inclined-plate clarifying basin 9 swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
V-type sand filter 10 fills effective size of grain 0.90-1.0mm quartz sand filtrate, filter tank total inflow 4000-5000m
3/ h, filtering velocity 7.0-8.0m/h.
R/O topping-up pump 12 total flux 3500-4500 m
3/ h; High efficiency filter 13 diameter 2000-4000mm, flow velocity 35-40m/h; Cartridge filter 14 is PP filter core cartridge filter, filtering accuracy 4-6 μm.
5. step 2.-4. in concentrated seawater enter salt making system 20 carry out salt manufacturing and chlor-alkali devices 21 produces chlorine and caustic soda by carrying bromine device 19, fresh water enters pure water after-treatment system 17, is used as tap water or boiler feedwater after treatment.
Table 4 is depicted as the parameter of hotting mask coproduction described in embodiment 3.
Table 4
。
Table 5 is depicted as power consumption and the relevant volume situation of embrane method production described in embodiment 3.
Table 5
。
Claims (9)
1. the method for a hotting mask co-production sea water desalination, comprise power plant's salt water cooling system, power plant's Deuslfurizing system for sea water and seawater desalination system, it is characterized in that, use the pre-hot sea water of power-plant flue gas waste heat, then enter desalination system and desalinate, desalination system adopts hot method desalination system and the parallel connection of embrane method desalination system, through the concentrated seawater of desalination system by carrying bromine device and enter salt making system and chlor-alkali devices preparing salt, chlorine and caustic soda, idiographic flow is:
1. seawater is drawn into power plant's salt water cooling system by sea-water pump, and seawater divides three routes to process afterwards;
2. Article 1 route, seawater enters power plant's Deuslfurizing system for sea water, and power plant's Deuslfurizing system for sea water is connected with power-plant flue gas bootstrap system, enters power plant's Deuslfurizing system for sea water after the power-plant flue gas in power-plant flue gas bootstrap system and seawater to make heat exchange;
3. Article 2 route, seawater enters power-plant flue gas bootstrap system, carry out countercurrent flow at this seawater and the power-plant flue gas of 140-150 DEG C come from boiler of power plant, enter Deuslfurizing system for sea water, the seawater after intensification enters low-temperature multi-effect desalting equipment and/or multistage flash evaporation desalting equipment is desalinated;
4. Article 3 route, embrane method desalination system: seawater enters sea-water reverse osmose apparatus;
5. step 2.-4. in concentrated seawater enter salt making system and carry out salt manufacturing and chlor-alkali devices by carrying bromine device and produce chlorine and caustic soda, fresh water enters pure water after-treatment system, is used as tap water or boiler feedwater after treatment.
2. the method for a kind of hotting mask co-production sea water desalination according to claim 1, is characterized in that, step 1. in seawater reach 24-35 DEG C through power plant's salt water cooling system temperature.
3. the method for a kind of hotting mask co-production sea water desalination according to claim 1, is characterized in that, step 3. at power-plant flue gas bootstrap system, the power-plant flue gas temperature after heat exchange reaches 100-110 DEG C, and the seawater temperature after heat exchange reaches 60-80 DEG C.
4. the method for a kind of hotting mask co-production sea water desalination according to claim 1, is characterized in that, step 4. in sea-water reverse osmose apparatus comprise pretreatment unit and desalting equipment.
5. the method for a kind of hotting mask co-production sea water desalination according to claim 4, is characterized in that, pretreatment unit comprises that water conservancy diversion is micro-revolves reaction tank, inclined-plate clarifying basin, V-type sand-bed filter, clean water basin, R/O topping-up pump, high efficiency filter and cartridge filter; Desalting equipment comprises high pressure water pump and film desalting equipment.
6. the method for a kind of hotting mask co-production sea water desalination according to claim 5, is characterized in that, seawater enters that water conservancy diversion is micro-revolves reaction tank, carry out flocculation reaction, the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reducing gradually, is 0.1-0.5m/s to flow velocity during outlet.
7. the method for a kind of hotting mask co-production sea water desalination according to claim 5, is characterized in that, inclined-plate clarifying basin swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
8. the method for a kind of hotting mask co-production sea water desalination according to claim 5, is characterized in that, effective size of grain 0.9-1.0mm quartz sand filtrate filled by V-type sand-bed filter, and sand-bed filter total inflow is 4000-5000m
3/ h, filtering velocity 7.0-8.0m/h.
9. the method for a kind of hotting mask co-production sea water desalination according to claim 5, is characterized in that, R/O topping-up pump total flux 3500-4500 m
3/ h; High efficiency filter diameter 2000-4000mm, flow velocity 35-40m/h; Cartridge filter is PP filter core cartridge filter, filtering accuracy 4-6 μm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310420656.4A CN103508603B (en) | 2013-09-16 | 2013-09-16 | Hot-membrane co-production sea water desalination method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310420656.4A CN103508603B (en) | 2013-09-16 | 2013-09-16 | Hot-membrane co-production sea water desalination method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103508603A CN103508603A (en) | 2014-01-15 |
| CN103508603B true CN103508603B (en) | 2015-06-03 |
Family
ID=49892098
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310420656.4A Active CN103508603B (en) | 2013-09-16 | 2013-09-16 | Hot-membrane co-production sea water desalination method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103508603B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355471B (en) * | 2014-10-21 | 2016-06-08 | 北京北控海创科技有限公司 | A kind of hotting mask coupling seawater desalination system and technique |
| CN111392830A (en) * | 2020-04-01 | 2020-07-10 | 青岛双瑞海洋环境工程股份有限公司 | Integrated refinery seawater cooling system |
| CN114506950A (en) * | 2020-11-16 | 2022-05-17 | 中国石油化工股份有限公司 | Zero-discharge method for sewage of refining enterprises |
| CN112520903A (en) * | 2020-12-18 | 2021-03-19 | 哈尔滨工业大学水资源国家工程研究中心有限公司 | Seawater desalination pretreatment system and use method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101081706A (en) * | 2006-12-27 | 2007-12-05 | 韩建民 | Electricity, salt and water co-production sea water desalination system |
| CN101143754A (en) * | 2007-06-04 | 2008-03-19 | 葛文宇 | Circulation extraction, zero discharging, comprehensive utilization, energy-saving and low-cost sea water desalination method |
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6186989A (en) * | 1984-10-02 | 1986-05-02 | Ishikawajima Harima Heavy Ind Co Ltd | Seawater desalting composite equipment |
-
2013
- 2013-09-16 CN CN201310420656.4A patent/CN103508603B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101081706A (en) * | 2006-12-27 | 2007-12-05 | 韩建民 | Electricity, salt and water co-production sea water desalination system |
| CN101143754A (en) * | 2007-06-04 | 2008-03-19 | 葛文宇 | Circulation extraction, zero discharging, comprehensive utilization, energy-saving and low-cost sea water desalination method |
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103508603A (en) | 2014-01-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102583839B (en) | Integrated method for seawater desalination, salt manufacturing and heat and electricity generation | |
| CN203269703U (en) | System for producing fresh water and salt production raw material by desalinating seawater in novel membrane method | |
| CN203269704U (en) | Raw material coupling system for preparing fresh water and salt by using seawater through membrane method | |
| CN103508603B (en) | Hot-membrane co-production sea water desalination method | |
| CN102329018A (en) | Device for desalting sea water by low-pressure membrane method | |
| CN203866137U (en) | Direct drinking water purification system for building pipeline | |
| CN101462804A (en) | Electromembrane seawater desalination method and complete set of equipment | |
| CN201309871Y (en) | Miniature seawater desalination device | |
| CN103408179A (en) | Production method for desalting seawater by hot film coupling | |
| CN104817134A (en) | Full-membrane method seawater desalting integration system adopting ultrafiltration-nanofiltration-reverse osmosis, and full-membrane method seawater desalting integration process adopting ultrafiltration-nanofiltration-reverse osmosis | |
| CN102757138B (en) | Seawater desalination treatment method adopting combination of wind energy power generation and salt chemical industry | |
| CN107117756B (en) | A kind of hotting mask coupling desalination process | |
| CN104326590B (en) | A kind of method and device thereof that utilizes preparing salt by working up seawater | |
| CN104445761A (en) | Energy-saving seawater purification equipment | |
| CN102745852B (en) | Brine-desalination method | |
| CN101781041A (en) | Method for desalting bitter by electromembrane method and equipment thereof | |
| CN207608448U (en) | Utilize the seawater desalination system of power station thermal energy production and living water | |
| CN106800351A (en) | Full Membrane seawater desalination and strong brine utilization system | |
| CN204569566U (en) | A kind of sea water desaltination utilization system | |
| CN203513418U (en) | Hot-membrane cogeneration system | |
| WO2013134901A1 (en) | Sea water desalination processing system | |
| CN204981442U (en) | Seawater desalination integrated equipment | |
| CN106986489A (en) | A kind of hotting mask couples seawater desalination system | |
| CN202297261U (en) | Sea water desalination device using low-pressure membrane method | |
| CN206858348U (en) | A kind of hotting mask couples seawater desalination system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |