CN203513418U - Hot-membrane cogeneration system - Google Patents
Hot-membrane cogeneration system Download PDFInfo
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- CN203513418U CN203513418U CN201320572301.2U CN201320572301U CN203513418U CN 203513418 U CN203513418 U CN 203513418U CN 201320572301 U CN201320572301 U CN 201320572301U CN 203513418 U CN203513418 U CN 203513418U
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- water
- seawater
- power plant
- desalting equipment
- desalination
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- 239000012528 membrane Substances 0.000 title abstract description 8
- 239000013535 sea water Substances 0.000 claims abstract description 112
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 51
- 238000010612 desalination reaction Methods 0.000 claims abstract description 34
- 150000003839 salts Chemical class 0.000 claims abstract description 29
- 238000001816 cooling Methods 0.000 claims abstract description 19
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims abstract description 12
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052794 bromium Inorganic materials 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 10
- 238000011033 desalting Methods 0.000 claims description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 29
- 239000003546 flue gas Substances 0.000 claims description 29
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 8
- 239000004576 sand Substances 0.000 claims description 6
- 239000006004 Quartz sand Substances 0.000 claims description 5
- 239000000706 filtrate Substances 0.000 claims description 5
- 230000004907 flux Effects 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000000779 smoke Substances 0.000 abstract description 3
- 239000002912 waste gas Substances 0.000 abstract description 3
- 230000007547 defect Effects 0.000 abstract description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract 1
- 230000023556 desulfurization Effects 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000013505 freshwater Substances 0.000 description 11
- 238000001223 reverse osmosis Methods 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 229910052801 chlorine Inorganic materials 0.000 description 5
- 239000000460 chlorine Substances 0.000 description 5
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000005189 flocculation Methods 0.000 description 4
- 230000016615 flocculation Effects 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 4
- 239000008399 tap water Substances 0.000 description 4
- 235000020679 tap water Nutrition 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 230000007812 deficiency Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model relates to a hot-membrane cogeneration system. The hot-membrane cogeneration system comprises a power plant seawater cooling system, a power plant seawater desulfurization system, a power plant smoke waste heat system and a seawater desalination system, wherein the seawater is preheated by using waste heat of gas in a power plant smoke flue, and then the seawater enters the desalination system to be desalinated; the desalination system adopts a hot process desalination system and a membrane process desalination system connected in parallel, so that defects of independent utilization of the hot process and the membrane process are avoided; the waste heat of the waste gas is fully used, so that water requirements in different regions and seasons are met, the desalination cost is reduced and the environmental thermal pollution is reduced; salinity of the desalinated seawater is 3.5-4%; and compared with the ordinary seawater, the yield of the salt is increased by more than 30% and the production cost of bromine is reduced by about 50%.
Description
Technical field
The utility model belongs to field of sea water desalting technology, has been specifically related to a kind of hotting mask co-generation system, and the mode that instant heating method and embrane method combine, meets different water demands, 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 is more than 28,000 hundred million m
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 are seriously polluted, 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, to 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 that heating of seawater is evaporated, make again vapor condensation obtain the process of fresh water, simple to operate, but cost is high, and energy consumption is large.Embrane method is mainly reverse osmosis (RO) technology, reverse osmosis method claims again ultra-filtration method conventionally, it is to utilize semi-permeable membranes, under pressure, allow water to see through and salinity and impurity are held back, although reverse osmosis method method of specific heat aspect energy consumption is low by 10%～20%, because membrane resistance is large, in servicely need to use high-pressure pump, and film is expensive, the life-span is short, has every year 50% decay; 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 is had relatively high expectations to sea water preprocessing, seawater region, water temperature variation in season.
In a word, high cost is the important factor of the domestic sea water desaltination development of at present restriction, is also the major reason that desalination water cannot large-scale promotion.How two kinds of methods are combined and respectively get the chief and overcome two kinds of methods shortcoming separately, comprehensive its advantage, and the concentrated seawater after desalination is made full use of, be the problem that the utility model need to solve.
Summary of the invention
The purpose of this utility model is exactly to provide a kind of hotting mask co-generation system for the defect of above-mentioned existence.This process costs is low, overcome hot method and embrane method and used separately the deficiency of existence, take full advantage of waste gas residual heat, different geographical, the water demand in season have been met, reduced fresh water cost, reduced environmental thermal pollution, for coastland, particularly the city of shortage of fresh water has more important application value.
A kind of hotting mask co-generation system technical scheme of the present utility model is, comprise power plant's salt water cooling system, power plant's Deuslfurizing system for sea water, and seawater desalination system, sea-water pump is connected with desalination system and is connected by electric power plant cooling system, desalination system is that hot method desalination system and embrane method desalination system are in parallel, and desalination system is connected with chlor-alkali device with salt making system respectively by carrying bromine device.
The exit seawater temperature of power plant's salt water cooling system is 24-35 ℃.
Hot method desalination system comprises power plant's Deuslfurizing system for sea water and the power-plant flue gas bootstrap system being connected with electric power plant cooling system respectively, and wherein the exhaust gases passes of boiler of power plant is connected with power plant Deuslfurizing system for sea water by power-plant flue gas bootstrap system; The seawater passage of power-plant flue gas bootstrap system is also connected with multistage flash evaporation desalting equipment with low-temperature multi-effect desalting equipment respectively, and low-temperature multi-effect desalting equipment is connected with multistage flash evaporation desalting equipment.
The water outlet of low-temperature multi-effect desalting equipment and multistage flash evaporation desalting equipment is connected to pure water after-treatment system; The concentrated seawater outlet of low-temperature multi-effect desalting equipment, multistage flash evaporation desalting equipment and power plant's Deuslfurizing system for sea water is connected to carries bromine device.
The exhaust gases passes of power-plant flue gas bootstrap system and seawater passage are countercurrent heat exchange method, and power-plant flue gas bootstrap system gas approach temperature is 140-150 ℃, and exhanst gas outlet temperature is 100-110 ℃; Seawer outlet temperature is 60-80 ℃.
Embrane method desalination system comprises sea-water reverse osmose apparatus, sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment, and pretreatment unit comprises micro-reaction tank, inclined-plate clarifying basin, V-type sand-bed filter, clean water basin, R/O topping-up pump, high efficiency filter and the cartridge filter of revolving of water conservancy diversion connecting successively; Desalting equipment comprises high pressure water pump and film desalting equipment.
The micro-reaction tank that revolves of water conservancy diversion, inlet velocity is 0.5-1m/s, exit velocity is 0.1-0.5m/s.
Inclined-plate clarifying basin swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
V-type sand filter is filled 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 μ m.
This hotting mask co-generation system technical process is:
1. sea-water pump is drawn into power plant's salt water cooling system by seawater, and seawater divides three routes to process afterwards;
2. article one 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. second route, seawater enters power-plant flue gas bootstrap system, at this seawater and the flue gas of 140-150 ℃ coming from boiler of power plant, carry out countercurrent flow, 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. A Third Way line, embrane method desalination system: seawater enters sea-water reverse osmose apparatus;
5. step 2.-concentrated seawater in 4. enters by carrying bromine device that salt making system carries out salt manufacturing and chlor-alkali device is produced chlorine and caustic soda, fresh water enters pure water after-treatment system, after treatment as tap water or boiler feedwater.
The seawater of step in 1. reaches 24-35 ℃ 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 ℃, the seawater temperature after heat exchange reaches 60-80 ℃.
Step 4. middle sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment.
Pretreatment unit comprises micro-reaction tank, inclined-plate clarifying basin, V-type sand-bed filter, clean water basin, R/O topping-up pump, high efficiency filter and the cartridge filter of revolving of water conservancy diversion; Desalting equipment comprises high pressure water pump and film desalting equipment.
Seawater enters the micro-reaction tank that revolves of water conservancy diversion, carries out flocculation reaction, and the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, and flow velocity is 0.1-0.5m/s when exporting.
Preferably, seawater enters the micro-reaction tank that revolves of water conservancy diversion, carries out flocculation reaction, and the reaction times is 25 minutes, and inlet velocity is 0.5m/s, reduces gradually, and flow velocity is 0.2m/s when exporting.Inclined-plate clarifying basin swash plate length 1 m, settling tank upflow velocity 1.5mm/s; V-type sand filter is filled 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 μ m.
The beneficial effects of the utility model are: a kind of hotting mask co-generation system cost of the present utility model is low, overcome hot method and embrane method and used separately the deficiency of existence, take full advantage of waste gas residual heat, different geographical, the water demand in season have been met, reduced fresh water cost, reduced environmental thermal pollution, the concentrated seawater salinity after desalination is 3.5-4%, salt output can improve more than 30% than common seawater, produces bromine than about 50% left and right of common seawater cost.
A kind of hotting mask co-generation system feature of the present utility model:
1, less investment: the 1/2-2/3 that investment cost is other techniques;
2, energy consumption is low: lower more than 20% than other techniques;
3, to seawater strong adaptability, equipment mobility is strong.
A kind of hotting mask co-generation system economic target of the present utility model:
1, ratio of desalinization 99.7%;
2, the water rate of recovery 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 simple hot method running cost is 7 yuan of left and right, and simple reverse osmosis method running cost is 5 yuan of left and right.
accompanying drawing explanation:
Figure 1 shows that process flow diagram of the present utility model.
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, the 8. micro-reaction tank that revolves of water conservancy diversion, 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 better the utility model, with specific examples, describe the technical solution of the utility model in detail below, but the utility model is not limited to this.
A kind of hotting mask co-generation system of the present utility model, 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 station stack gas waste heat, then enter desalination system and 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 device being prepared salt, chlorine and caustic soda.
Hot method is produced
1. sea-water pump 1 is drawn into power plant's salt water cooling system 2 by seawater, and seawater reaches 24-35 ℃ through power plant's salt water cooling system 2 temperature, and seawater is processed through following route afterwards;
2. article one 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. second route, seawater enters power-plant flue gas bootstrap system 4, at this seawater and the flue gas of 140-150 ℃ coming from boiler of power plant, carry out countercurrent flow, flue-gas temperature after heat exchange reaches 100-110 ℃, seawater temperature after heat exchange reaches 60-80 ℃, 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. the concentrated seawater of step 2., in 3. enters by carrying bromine device 19 that salt making system 20 carries out salt manufacturing and chlor-alkali device 21 is produced chlorine and caustic soda, and fresh water enters pure water after-treatment system 17, after treatment as tap water or boiler feedwater.
Table 1 is depicted as parameter and the power consumption situation that hot method is produced described in embodiment 1.
Table 1
embodiment 2
Embrane method is produced
1. sea-water pump 1 is drawn into power plant's salt water cooling system 2 by seawater, and seawater reaches 24-35 ℃ through power plant's salt water cooling system 2 temperature;
2. embrane method desalination system: seawater enters sea-water reverse osmose apparatus, and sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment; Pretreatment unit comprises micro-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 the cartridge filter 14 of revolving of water conservancy diversion; Desalting equipment comprises high pressure water pump 15, energy recycle device and boost in pressure system and film desalting equipment 16.
Seawater enters the micro-reaction tank 8 that revolves of water conservancy diversion, carries out flocculation reaction, and the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, and flow velocity is 0.1-0.5m/s when exporting.
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 is filled 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 μ m.
3. the concentrated seawater of step in 2. enters by carrying bromine device 19 that salt making system 20 carries out salt manufacturing and chlor-alkali device 21 is produced chlorine and caustic soda, and fresh water enters pure water after-treatment system 17, after treatment as tap water or boiler feedwater.
Table 2 is depicted as the parameter that embrane method is produced described in embodiment 2.
Table 2
。
Table 3 is depicted as power consumption and the relevant output situation that embrane method is produced described in embodiment 2.
Table 3
embodiment 3
Hotting mask coproduction
1. sea-water pump 1 is drawn into power plant's salt water cooling system 2 by seawater, and seawater reaches 24-35 ℃ through power plant's salt water cooling system 2 temperature, and seawater is processed through following route simultaneously afterwards;
2. article one 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. second route, seawater enters power-plant flue gas bootstrap system 4, at this seawater and the flue gas of 140-150 ℃ coming from boiler of power plant, carry out countercurrent flow, flue-gas temperature after heat exchange reaches 100-110 ℃, seawater temperature after heat exchange reaches 60-80 ℃, 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. A Third Way line, 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 micro-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 the cartridge filter 14 of revolving of water conservancy diversion; Desalting equipment comprises high pressure water pump 15, energy recycle device and boost in pressure system and film desalting equipment 16.
Seawater enters the micro-reaction tank 8 that revolves of water conservancy diversion, carries out flocculation reaction, and the reaction times is 20-30 minute, and inlet velocity is 0.5-1m/s, reduces gradually, and flow velocity is 0.1-0.5m/s when exporting.
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 is filled 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 μ m.
5. step 2.-concentrated seawater in 4. enters by carrying bromine device 19 that salt making system 20 carries out salt manufacturing and chlor-alkali device 21 is produced chlorine and caustic soda, fresh water enters pure water after-treatment system 17, after treatment as tap water or boiler feedwater.
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 output situation that embrane method is produced described in embodiment 3.
Table 5
Claims (10)
1. a hotting mask co-generation system, 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, sea-water pump is connected with desalination system and is connected by electric power plant cooling system, and desalination system is that hot method desalination system and embrane method desalination system are in parallel, and desalination system is connected with chlor-alkali device with salt making system respectively by carrying bromine device.
2. a kind of hotting mask co-generation system according to claim 1, is characterized in that, the exit seawater temperature of power plant's salt water cooling system is 24-35 ℃.
3. a kind of hotting mask co-generation system according to claim 1, it is characterized in that, hot method desalination system comprises power plant's Deuslfurizing system for sea water and the power-plant flue gas bootstrap system being connected with electric power plant cooling system respectively, and wherein the exhaust gases passes of boiler of power plant is connected with power plant Deuslfurizing system for sea water by power-plant flue gas bootstrap system; The seawater passage of power-plant flue gas bootstrap system is also connected with multistage flash evaporation desalting equipment with low-temperature multi-effect desalting equipment respectively, and low-temperature multi-effect desalting equipment is connected with multistage flash evaporation desalting equipment.
4. a kind of hotting mask co-generation system according to claim 3, is characterized in that, the water outlet of low-temperature multi-effect desalting equipment and multistage flash evaporation desalting equipment is connected to pure water after-treatment system; The concentrated seawater outlet of low-temperature multi-effect desalting equipment, multistage flash evaporation desalting equipment and power plant's Deuslfurizing system for sea water is connected to carries bromine device.
5. a kind of hotting mask co-generation system according to claim 3, it is characterized in that, the exhaust gases passes of power-plant flue gas bootstrap system and seawater passage are countercurrent heat exchange method, and power-plant flue gas bootstrap system gas approach temperature is 140-150 ℃, and exhanst gas outlet temperature is 100-110 ℃; Seawer outlet temperature is 60-80 ℃.
6. a kind of hotting mask co-generation system according to claim 1, it is characterized in that, embrane method desalination system comprises sea-water reverse osmose apparatus, sea-water reverse osmose apparatus comprises pretreatment unit and desalting equipment, and pretreatment unit comprises micro-reaction tank, inclined-plate clarifying basin, V-type sand-bed filter, clean water basin, R/O topping-up pump, high efficiency filter and the cartridge filter of revolving of water conservancy diversion connecting successively; Desalting equipment comprises high pressure water pump and film desalting equipment.
7. a kind of hotting mask co-generation system according to claim 6, is characterized in that, the micro-reaction tank that revolves of water conservancy diversion, and inlet velocity is 0.5-1m/s, exit velocity is 0.1-0.5m/s.
8. a kind of hotting mask co-generation system according to claim 6, is characterized in that inclined-plate clarifying basin swash plate length 0.8-1.2m, settling tank upflow velocity 1.0-2.0mm/s.
9. a kind of hotting mask co-generation system according to claim 6, is characterized in that, V-type sand filter is filled 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.
10. a kind of hotting mask co-generation system according to claim 6, 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 μ m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320572301.2U CN203513418U (en) | 2013-09-16 | 2013-09-16 | Hot-membrane cogeneration system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320572301.2U CN203513418U (en) | 2013-09-16 | 2013-09-16 | Hot-membrane cogeneration system |
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| CN203513418U true CN203513418U (en) | 2014-04-02 |
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| CN201320572301.2U Expired - Fee Related CN203513418U (en) | 2013-09-16 | 2013-09-16 | Hot-membrane cogeneration system |
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| Country | Link |
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2013
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