CN103787434B - Condensing steam turbine generator group electricity, water, salt joint production process - Google Patents
Condensing steam turbine generator group electricity, water, salt joint production process Download PDFInfo
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- CN103787434B CN103787434B CN201310729374.2A CN201310729374A CN103787434B CN 103787434 B CN103787434 B CN 103787434B CN 201310729374 A CN201310729374 A CN 201310729374A CN 103787434 B CN103787434 B CN 103787434B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- 150000003839 salts Chemical class 0.000 title claims abstract description 25
- 230000005611 electricity Effects 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 238000000034 method Methods 0.000 claims abstract description 23
- 239000012267 brine Substances 0.000 claims abstract description 17
- 239000002826 coolant Substances 0.000 claims abstract description 17
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 17
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 15
- 239000013505 freshwater Substances 0.000 claims abstract description 9
- 239000003513 alkali Substances 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 235000017550 sodium carbonate Nutrition 0.000 claims abstract description 7
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims description 51
- 239000013535 sea water Substances 0.000 claims description 47
- 239000012266 salt solution Substances 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 9
- 238000007670 refining Methods 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 7
- 239000013589 supplement Substances 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 4
- 241001131796 Botaurus stellaris Species 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 238000007738 vacuum evaporation Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The present invention relates to condensing steam turbine generator group electricity, water, salt joint production process, be specially negative pressure steam that condensing steam turbine generator group discharges after generating be used for production liquid brine as raw material for chlor-alkali or the production of soda ash system, and coproduction fresh water. Condensing steam turbine generator group electricity, water, salt joint production process, comprise the following steps: the Steam Actuation condensing steam turbine generator group running that (1) upper level technique produces, thereby can generate electricity, be to enter heat exchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with the cooling medium heat exchange of extracting out from basin by forced circulation pump, tail steam is condensed into water, carries out returning to boiler water treatment system after vapor-liquid separation and recycle in block steam and drain water device. Condensing steam turbine generator group electricity of the present invention, water, salt joint production process, technique is simple, can realize electricity, salt, water coproduction.
Description
Technical field
The present invention relates to condensing steam turbine generator group electricity, water, salt joint production process, be specially condensing-type steamerThe negative pressure steam that generating set is discharged after generating is used for production liquid brine as raw material confession chlor-alkali or soda ashSystem production use, and coproduction fresh water.
Background technology
Thermal power generation at present is substantially divided into back pressure turbine generating, condensing turbine generating, takes out condensing-typeThree kinds of forms of steam turbine power generation, back pressure turbine generating feature is that steam turbine end steam discharge pressure is greater thanNormal pressure, the steam of discharge is commonly used for other technique (such as warming), and its generating efficiency is lower than condensing-typeSteam turbine power generation and take out condensing-type steamer generating, but the latent heat enthalpy of steam is utilized substantially; Condensing-type steamerMachine generating feature is: steam turbine end discharge pressure is lower than normal pressure, i.e. negative pressure state, and generating efficiency is the highest,But the latent heat enthalpy of steam is not utilized, the heat utilization rate less than 45% of whole system, takes out condensing-type steamerGenerator between above-mentioned two kinds of techniques, is characterized in extracting out and having certain pressure from steam turbine intergradeThe hot user of steam supply, remaining steam continues the blade acting at drive rotor rear portion, then reclaims condensed water.Because the steam latent heat enthalpy of extracting part out has obtained utilization, and the steam enthalpy of condensation portion is not utilized,Therefore its utilization efficiency of heat energy is between back pressure type generating set and condensing-type generating set.
As the vacuum method salt manufacturing of one of crude salt mode of production, mostly combine with thermal power plant, utilize the back of the bodyThe malleation steam that pressure type generating set or bleeder generating set are discharged adopts multiple-effect cryogenic vacuum evaporation technology rawProduce crude salt, the feature of this technique is: although steam latent heat is fully utilized, generating efficiencyLow.
Have more producer to adopt seawater as cooling water near coastal thermal power plant, its type of cooling canBe divided into single flow and circulating, single flow refers to that seawater is straight after the heat of cooling and absorbing generating set steamRun in, after the circulating heat that refers to cooled with seawater absorption generating set steam, send into cooling tower, through coolAfter water tower cooling, recycle, due to concentrating of cooling tower, salinity improves constantly, and therefore needs timing to dischargeDense seawater supplements into fresh seawater simultaneously. No matter which kind of mode is used seawater, useful one-tenth in its seawaterPart is not effectively utilized.
Its discharge of condensing-type generating set and steam-extracting type generating set (below taking condensing-type generating set as example)Vapor (steam) temperature be generally no more than 50 DEG C summer, the winter in the north can be lower. The steam that steam turbine is dischargedThe water-cooled that is cooled is congealed into after water and is returned to steam generator system, and therefore the contained heat energy of this part steam does not obtain effectivelyUtilize.
Summary of the invention
For the deficiencies in the prior art, the object of the present invention is to provide a kind of heat utilization rate high,Condensing steam turbine generator group electricity, water, salt joint production process that seawater can get utilization.
The present invention is achieved by the following technical solutions:
Condensing steam turbine generator group electricity, water, salt joint production process, its special character is to comprise the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thus can generate electricity,Be to enter heat exchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with logicalCross the cooling medium heat exchange that forced circulation pump is extracted out from basin, tail steam is condensed into water, at block steam and drain waterIn device, carrying out returning to boiler water treatment system after vapor-liquid separation recycles;
(2) cooling medium (temperature is above the boiling point) after heated enters vapour liquid separator, owing to isolatingSteam and concentrating, in the time that in isolated liquid, salinity reaches 300g/l～310g/l, a part of liquid warpForced circulation pump is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine, and remainder supplements with newThe cooling medium of coming in is sent into heat exchanger after mixing and is recycled;
(3) enter surface condenser from the isolated indirect steam of vapour liquid separator, fresh through purified treatmentSeawater is added cooling tower, is pumped into surface condenser by recirculated cooling water, and with indirect steam heat exchange, secondary steamsVapour is condensed into fresh water and delivers to water pipe network, taken away by vavuum pump from surface condenser fixed gas out,Absorb circulating cooling seawater reflux after heat to cooling tower, after cooling with newly add come in through purified treatmentFresh seawater send surface condenser to recycle after mixing again;
Described cooling medium is bittern or Industry Waste salt solution;
Described cooling medium be through seawater refining system refining, from the circulating cooling seawater of cooling tower.
Condensing steam turbine generator group electricity of the present invention, water, salt joint production process, technique is simple, can realize electricity,Salt, water coproduction, if combined with sea water desalinating unit, chlor-alkali (or soda ash) process units, not only canGreatly alleviate environmental pollution, accomplish utilization of waste as resource, and can supply high-quality fresh water outward, greatly improveEnergy utilization rate, take full advantage of the negative pressure steam that enthalpy is lower, with the loss of less generating efficiency, changeObtained high-quality fresh water and industrial salt, the fresh water that only obtained is worth the value just reducing higher than loss generating.
Brief description of the drawings
Fig. 1: condensing steam turbine generator group electricity of the present invention, water, salt joint production process flow chart;
In figure: 1, condensing steam turbine generator group, 2, heat exchanger, 3, block steam and drain water device, 4, boiler waterTreatment system, 5, vapour liquid separator, 6, forced circulation pump, 7, chlor-alkali or soda ash system, 8, force to followRing pump, 9, basin, 10, surface condenser, 11, vavuum pump, 12, water pipe network, 13, cooling tower,14, circulating cooling water pump, 15, seawater refining system.
Detailed description of the invention
Further illustrate method provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention is not subject toAny restriction.
Condensing steam turbine generator group electricity, water, salt joint production process, comprise the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thus can generate electricity,Be to enter heat exchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with logicalCross the cooling medium heat exchange that forced circulation pump is extracted out from basin, tail steam is condensed into water, at block steam and drain waterIn device, carrying out returning to boiler water treatment system after vapor-liquid separation recycles;
(2) cooling medium (temperature is above the boiling point) after heated enters vapour liquid separator, owing to isolatingSteam and concentrating, in the time that in isolated liquid, salinity reaches 300g/l～310g/l, a part of liquid warpForced circulation pump is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine, and remainder supplements with newThe cooling medium of coming in is sent into heat exchanger after mixing and is recycled;
(3) enter surface condenser from the isolated indirect steam of vapour liquid separator, fresh through purified treatmentSeawater is added cooling tower, is pumped into surface condenser by recirculated cooling water, and with indirect steam heat exchange, secondary steamsVapour is condensed into fresh water and delivers to water pipe network, taken away by vavuum pump from surface condenser fixed gas out,Absorb circulating cooling seawater reflux after heat to cooling tower, after cooling with newly add come in through purified treatmentFresh seawater send surface condenser to recycle after mixing again;
Described cooling medium be through seawater refining system refining, from the circulating cooling seawater of cooling tower.
The present embodiment be first by through seawater refining system refining, do from the circulating cooling seawater of cooling towerFor cooling medium carrys out the steam that cooling steam turbine is discharged, after Steam Heating seawater, itself is condensed into water,In block steam and drain water device, carry out returning to boiler water treatment system after vapor-liquid separation and recycle, after Absorption by Sea Water heatTemperature raises, and the seawater that temperature exceedes after boiling point removes vapour liquid separator, and the indirect steam of separating goes to surfaceCondenser, is become fresh water to remove water pipe network by the circulating cooling seawater condensing from cooling tower, and contained is not solidifyingGas is taken away by vavuum pump, and the seawater after vapor-liquid separation is extracted out by forced circulation pump, when salinity in seawater reachesAfter 300g/l～310g/l, become the liquid brine that salt content is qualified, extract a part of refined brine out as raw material saltWater send chlor-alkali production system or soda ash production system, and remainder continues circulation with the sea water mixing of supplementing intoHeating, concentrated production liquid brine.
The kind of cooling tower can be selected existing any form such as open type, enclosed and technology, makes circulating cooling seaWater reduces temperature by the mode of transpiring moisture, and along with the evaporation of moisture, salinity raises gradually, add fromThe seawater that circulating cooling system is extracted some out removes to produce refined brine, therefore needs constantly in system, to supplementFresh seawater.
Supplement into the seawater in cooling tower and need carry out purified treatment, in case cooling tower fouling.
Heat exchanger can adopt any type of heat exchanger, the preferred shell and tube of heat exchanger or plate type heat exchanger. Along withThe carrying out of heat exchange, brine temp raises. When NaCl content in salt solution is gas in 310g/l, vapour liquid separatorPhase pressure is-when 0.08MPa (gauge pressure), the about 67 DEG C of left and right of salt solution just come to life, under normal circumstances, salt solutionSalt content is low, and the boiling point of salt solution reduces, vacuum up, and salt water boiling point also reduces, when NaCl in salt solution containsAmount is for 310g/l, and when be increased to-0.09MPa of vacuum (gauge pressure), approximately 52 DEG C of salt solution will seethe with excitement.
Block steam and drain water device can adopt any type of block steam and drain water device, with reach only allow aqueous water discharge andThe object that does not allow steam to discharge.
Vapour liquid separator can adopt any type of vapor-liquid separating device, to reach the object of vapor-liquid separation.
Heat exchanger and vapour liquid separator also can adopt unitized, such as: levin evaporator, standard evaporationDevice etc.
The mode vacuumizing can be mechanical type, can be also water-jet formula.
Seawater circulating cooling mode and existing technique are basic identical, and difference is existing process of circulation cooling waterIn, along with the operation of producing, in refrigerated sea water, the cycles of concentration of salt will progressively increase, and therefore, require timingOutside cooling system, discharge the denseer seawater of a part, in case cooling system fouling needs toward circulating cooling simultaneouslySystem is constantly supplemented fresh seawater, to ensure system stable operation. Feature of the present invention is continuously from followingIn ring cooling system, extract the denseer seawater of part out, be transferred to next step and go to produce the liquid state that salt concentration is qualifiedSalt solution supplements fresh seawater simultaneously continuously in the interior system of cooling tower, and supplementary seawater amount is by producing refined saltThe amount of the needed seawater amount of water and cooling tower transpiring moisture determines.
The steam of discharging from steam turbine end is different from existing condensing steam turbine generator technique with temperature. ExistingThe steam that some condensing steam turbine generator ends is discharged directly removes surface condenser, by the recirculated water cooling liquid that congeals intoState water, condensate water is returned to boiler water treatment system again, and the vapor (steam) temperature of discharge is generally no more than 50 DEG C summer,The negative pressure of its generation is in the case of the heat exchange area of surface condenser is certain, mainly by the number of recirculated cooling waterAmount and temperature decision, under the certain condition of cooling water quantity, coolant water temperature is lower, and vacuum is higher. ThisThe bright steam that is condensing turbine is discharged is first sent heat exchanger to, and heating comes self-circulation cooling system and process placeThe seawater of reason, the water condensing into returns to boiler water treatment system after block steam and drain water device again, and exhaust temperature is generalBe greater than 65 DEG C, be less than 100 DEG C, the negative pressure of its generation is in the situation that heat exchange area is certain, mainly by heatedThe quantity of salt solution and temperature determine, control vapor (steam) temperature preferably≤85 DEG C.
Seawater in hydronic process, the indirect steam pressure that its boiling point is mainly discharged by vapour liquid separatorDetermine with the salinity in salt solution, and the pressure of indirect steam is determined (to be equivalent to existing by surface condenserThe technique of group of motors and technology). Brine strength is lower, and boiling point is lower. Under the certain condition of brine strength,Indirect steam pressure lower (that is: vacuum is higher), the boiling point of salt solution is lower, thereby makes Steam Turbine rowThe steam pressure and the temperature that go out are lower, and generating efficiency is just higher. Indirect steam must be controlled in process of production trueBe not less than-0.08MPa of reciprocal of duty cycle, (vacuum is more high better), in finished product salt solution, NaCl content is300g/1～310g/l, if lower than this scope, must continue circulating-heating concentrated, and height goes beyond the scope, and must addLarge qualified salt solution extracted amount.
Taking out from circulating cooling system mode that seawater removes to produce salt solution can adopt and directly send outside from cooling water pumpMode, also can install separately a water pump and specialize in production salt solution.
Can be treated cold from cooling tower circulation for the production of the raw material (cooling medium) of refined brineBut strong brine, the bittern etc. after seawater, the desalinization of system can be also to produce epoxychloropropane, MDIAnd the brine waste of other products by-product, or ionic membrane method produces the dechlorination light salt brine in caustic soda process,Or combination between them and supplementing. But, no matter what does raw material with, must ensure all raw materialsAfter heating is concentrated, must not produce fouling (with cooling tower circulating cooling system), concrete processing mode (such asSaying ion-exchange-resin process etc.) the present invention is not discussed.
The present invention is except can production liquid brine, and the mode that can also crystallizer be installed by increase is producedSolid state crystallization salt.
The present invention can separate cooling tower circulating cooling system to make with steam turbine exhaust steam heating concentration systemsWith, that is: existing cooling tower process of circulation cooling water is constant, discharges separately with Turbo-generator Set steam turbineNegative pressure Steam Heating concentrates production liquid brine.
The unspecified content of the present invention is prior art, and those skilled in the art can be from the present embodimentAnd prior art acquisition inspiration, be out of shape and obtain other embodiment. Therefore, protection scope of the present invention shouldThis protection domain according to claim is determined.
Claims (1)
1. condensing steam turbine generator group electricity, water, salt joint production process, is characterized in that comprising the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thus can generate electricity,Be to enter heat exchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with logicalCross the cooling medium heat exchange that forced circulation pump is extracted out from basin, tail steam is condensed into water, at block steam and drain waterIn device, carrying out returning to boiler water treatment system after vapor-liquid separation recycles;
(2) cooling medium after heated, temperature is above the boiling point, and enters vapour liquid separator, owing to isolatingSteam and concentrating, in the time that in isolated liquid, salinity reaches 300g/L～310g/L, a part of liquid warpForced circulation pump is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine, and remainder supplements with newThe cooling medium of coming in is sent into heat exchanger after mixing and is recycled;
(3) enter surface condenser from the isolated indirect steam of vapour liquid separator, fresh through purified treatmentSeawater is added cooling tower, is pumped into surface condenser by recirculated cooling water, and with indirect steam heat exchange, secondary steamsVapour is condensed into fresh water and delivers to water pipe network, taken away by vavuum pump from surface condenser fixed gas out,Absorb circulating cooling seawater reflux after heat to cooling tower, after cooling with newly add come in through purified treatmentFresh seawater send surface condenser to recycle after mixing again;
Described cooling medium is the seawater after seawater refining system is refining from the circulating cooling seawater of cooling towerOr bittern or Industry Waste salt solution.
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| CN201310729374.2A CN103787434B (en) | 2013-12-19 | 2013-12-19 | Condensing steam turbine generator group electricity, water, salt joint production process |
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| CN103787434B true CN103787434B (en) | 2016-05-18 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105314655B (en) * | 2015-10-19 | 2017-01-11 | 中盐榆林盐化有限公司 | Method and device for utilizing brine geothermal energy and condensed water heat energy |
| CN105923873B (en) * | 2016-05-26 | 2018-12-18 | 潘庆光 | A kind of processing method for the effluent brine that carbimide production system generates |
| CN107823909B (en) * | 2017-10-23 | 2023-12-01 | 江苏江锅智能装备股份有限公司 | Reboiler for distillation tower |
| CN107796237A (en) * | 2017-11-30 | 2018-03-13 | 无锡弘鼎华化工设备有限公司 | negative pressure steam heating method and system |
| CN110926049B (en) * | 2019-12-05 | 2023-11-21 | 陕西鼓风机（集团）有限公司 | Cogeneration low-temperature heating process and system |
| CN114922699A (en) * | 2022-05-11 | 2022-08-19 | 首钢京唐钢铁联合有限责任公司 | Cooling system of boiler steam turbine generator unit and control method |
Citations (5)
| 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 |
| CN102557168A (en) * | 2011-12-05 | 2012-07-11 | 北京朗新明环保科技有限公司 | Heat-pipe low-temperature multi-effect sea water desalinating system and process flow |
| CN102583857A (en) * | 2012-02-07 | 2012-07-18 | 绍兴文理学院 | Electrical fresh water co-production device for coastal thermal power plant and island thermal power plant |
| TW201235304A (en) * | 2011-02-25 | 2012-09-01 | Sasakura Eng Co Ltd | Water desalination device and water desalination method |
| CN102992422A (en) * | 2012-10-31 | 2013-03-27 | 南京紫晶藤节能科技有限公司 | Batch-type small-temperature difference heat-pump low-temperature seawater desalting system and method |
-
2013
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Patent Citations (5)
| 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 |
| TW201235304A (en) * | 2011-02-25 | 2012-09-01 | Sasakura Eng Co Ltd | Water desalination device and water desalination method |
| CN102557168A (en) * | 2011-12-05 | 2012-07-11 | 北京朗新明环保科技有限公司 | Heat-pipe low-temperature multi-effect sea water desalinating system and process flow |
| CN102583857A (en) * | 2012-02-07 | 2012-07-18 | 绍兴文理学院 | Electrical fresh water co-production device for coastal thermal power plant and island thermal power plant |
| CN102992422A (en) * | 2012-10-31 | 2013-03-27 | 南京紫晶藤节能科技有限公司 | Batch-type small-temperature difference heat-pump low-temperature seawater desalting system and method |
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