CN201587871U - Multi-stage vacuum distillation seawater desalination device - Google Patents
Multi-stage vacuum distillation seawater desalination device Download PDFInfo
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- CN201587871U CN201587871U CN2009202702592U CN200920270259U CN201587871U CN 201587871 U CN201587871 U CN 201587871U CN 2009202702592 U CN2009202702592 U CN 2009202702592U CN 200920270259 U CN200920270259 U CN 200920270259U CN 201587871 U CN201587871 U CN 201587871U
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- seawater
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- 239000013535 sea water Substances 0.000 title claims abstract description 68
- 238000010612 desalination reaction Methods 0.000 title abstract description 6
- 238000005292 vacuum distillation Methods 0.000 title abstract description 3
- 239000013505 freshwater Substances 0.000 claims abstract description 42
- 239000006200 vaporizer Substances 0.000 claims description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000011084 recovery Methods 0.000 abstract description 9
- 239000002918 waste heat Substances 0.000 abstract description 9
- 238000005507 spraying Methods 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 15
- 230000003020 moisturizing effect Effects 0.000 description 12
- 238000001704 evaporation Methods 0.000 description 10
- 230000008020 evaporation Effects 0.000 description 10
- 230000000694 effects Effects 0.000 description 9
- 238000004821 distillation Methods 0.000 description 7
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000012153 distilled water Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000012267 brine Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000004087 circulation Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- -1 condenser Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000000502 dialysis Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
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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
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
一种多级真空蒸馏海水淡化装置，属于海水淡化技术领域。它由若干组串联的真空蒸馏器、加热器(1)、冷却器(12)，以及淡水余热回收换热器(20)组成，每组真空蒸馏器由蒸发器、冷凝器、淡水槽组成。前一级的冷凝器(4)浸没于后一级蒸发器(5)的海水中，前一级蒸发器(2)中的海水经过流量调节阀(14)流进下一级的蒸发器(5)中。常温海水首先进入冷却器(12)，然后进入淡水余热换热器(20)，最后通过流量调节阀(13)流进第一级真空蒸发器(2)。外界热源通过加热器(1)为本装置提供热能，对海水进行淡化，其优点是无海水喷淋装置、有淡水余热回收，排出的浓海水温度低、浓度可调节，因而电能消耗小、热效率高。
A multistage vacuum distillation seawater desalination device belongs to the technical field of seawater desalination. It consists of several sets of vacuum distillers connected in series, heaters (1), coolers (12), and fresh water waste heat recovery heat exchangers (20). Each set of vacuum distillers consists of an evaporator, a condenser, and a fresh water tank. The previous stage condenser (4) is submerged in the seawater of the rear stage evaporator (5), and the seawater in the previous stage evaporator (2) flows into the next stage evaporator ( 5) in. Normal-temperature seawater first enters the cooler (12), then enters the fresh water waste heat exchanger (20), and finally flows into the first-stage vacuum evaporator (2) through the flow regulating valve (13). The external heat source provides heat energy for the device through the heater (1) to desalinate the seawater. Its advantages are that there is no seawater spraying device, there is fresh water waste heat recovery, and the discharged concentrated seawater has low temperature and adjustable concentration, so the power consumption is small and the thermal efficiency is low. high.
Description
(1) technical field
The utility model relates to a kind of multilevel vacuum distilling sea water desalinating plant, is mainly used in seawater (or brackish water) desalination.Belong to field of sea water desalting technology.
(2) background technology
The method that seawater or brackish water are desalinated is a lot, and conventional method has distillation method, ion exchange method, dialysis, reverse osmosis membrane and cold method etc.The method that the most extensively is studied in distillation method and uses mainly is multistage flash evaporation (MSF) sea water desalinating plant and multi-effect distilling (MED) sea water desalinating plant.
Multistage flash evaporation (MSF) sea water desalinating plant is to utilize the waste heat in power plant, chemical plant continuously to extract the very little high-quality fresh water of total solids material content from seawater, as the process water and the large-scale municipal water use of production process.Accompanying drawing 1 is a kind of schematic diagram of multistage flash evaporation.
Flash principle is salt solution to be heated to introduce after the certain temperature in the container (being called flashing chamber) that pressure is lower than the corresponding saturation pressure of its temperature institute, owing to salt solution is in superheat state suddenly, promptly dodges anxious distillation (abbreviation flash distillation) wink.The steam that produces removes in the devaporation behind the drop by scum dredger, enters distiller and condenses into product fresh water, and the circulating brine that flows through the distiller tube bank simultaneously also is heated.Flashing chamber, scum dredger, distiller, fresh-water tank etc. constitute flash evaporator.Multistage flash evaporation is exactly to carry out said process in the container of a plurality of such ordered arrangement.
The feature of multi-effect distilling (MED) desalination technology is that horizontal pipe falling film evaporation device (or vertical tube falling-film evaporator) is together in series, and with a certain amount of steam input, by repeatedly evaporation and condensation, obtains being multiple times than the distilled water of heating steam amount.Accompanying drawing 2 is schematic diagrams of a kind of multi-effect distilling (MED) sea water desalinating plant.
Among Fig. 2, the charging seawater is preheated in the heat extraction condenser and outgases, and is divided into two bursts of logistics afterwards.One logistics flows back to the sea as cooling fluid after finishing cooling effect, one logistics becomes the feeding liquid of still-process in addition.
Feed liquid is introduced in heat-recovery section and respectively imitates in minimum one group of temperature after adding dirt dispersion agent.Sprinkling system is distributed to feed liquid spray on the overhead coil in each vaporizer, along overhead coil downwards with form of film in the free-pouring process, a part of seawater is vaporized owing to having absorbed in vaporizer the latent heat of condensed steam.By slight spissated residue feed liquid with pump be driven into vaporizer next the group in, the service temperature of this group than last one group higher, in new group, repeated evaporation and spray process again.Remaining feed liquid is then beaten forward, to the last leaves this effect group with the form of concentrated solution in the highest effect group of temperature.
First phlegma of imitating is collected, and the part of this distilled water turns back to vapour generator again, and the part that surpasses the living quantity of steam of input flow in the first container of a series of special containers, and each container all is connected to the condensation side that next low temperature is imitated.Make a part of distilled water produce flash distillation like this and remaining product water cooling is got off, heat is passed in the main body that recovery of heat imitates gone simultaneously.As distilled water, concentrated seawater is from a series of strong brine flash tank of the first stepped inflow of effect, and flash cooling is to reclaim its heat.After overcooling, strong brine is squeezed into the sea through the strong brine pump.
In above-mentioned dual mode sea water desalinating plant, the vapor temperature that the multistage flash evaporation sea water desalinating plant need be imported is higher, and temperature is low excessively to cause progression to reduce, and efficient reduces.Because 1 ton of fresh water of the every desalination of multistage flash evaporation sea water desalinating plant needs 8 tons of seawater circulations through this device, therefore must need powerful water circulating pump, its maximum shortcoming is exactly the energy consumption height.Effect distillation seawater desalinating device of multi then needs complicated seawater spraying system, sprinkling system is the key part of effect distillation seawater desalinating device of multi, spray flux evenly makes tube surface well wetting in the spray zone in vaporizer, non-uniform spraying will cause the local dried wall of heat-transfer surface, easily fouling, cause condenser early failure and heat-transfer effect to worsen, spray performance quality is directly connected to the safe operation of effect distillation seawater desalinating device of multi.Seawater is to flow to the first step from last step in effect distillation seawater desalinating device of multi, and the temperature that concentrated seawater is discharged is very high, must carry out waste heat recovery, therefore, and the manufacturing complexity of this method, manufacturing cost height.
(3) summary of the invention
In order to overcome the shortcoming of above-mentioned two kinds of sea water desalinating plants, the utility model provides a kind of does not have spray equipment, the multilevel vacuum distilling sea water desalinating plant of fresh water waste heat recovery is arranged, and its temperature of discharging concentrated seawater is low, concentration can be regulated; And the fresh water waste heat recovery has improved the moisturizing temperature of first evaporator, has eliminated surfusion.Thereby have low cost of manufacture, a advantage that thermo-efficiency is high.
The utility model is achieved in that
The multi-stage vacuum sea water desalinating plant is by some groups of placed in-line vacuum distilling apparatuses, water cooler, well heater, and the fresh water heat recovery heat exchanger is formed, every group of vacuum distilling apparatus is made up of vaporizer, condenser, fresh-water tank, the condenser of previous stage is immersed in the seawater of back one-level vaporizer, and the previous stage vaporizer links to each other with the vaporizer of next stage through flow control valve; The steam that the last step vaporizer produces enters the last step condenser that places in the water cooler; Normal temperature seawater at first enters water cooler, enters the fresh water afterheat heat exchanger then, enters in the first step vacuum-evaporator by flow control valve at last; Fresh water in the fresh-water tanks at different levels at first passes through the fresh water afterheat heat exchanger, is then taken away; And concentrated seawater is taken away, is discharged in the last step vaporizer.
(4) description of drawings
Fig. 1 is the schematic diagram of a kind of multistage flash evaporation (MSF) sea water desalinating plant.
Fig. 2 is the schematic diagram of a kind of multi-effect distilling (MED) sea water desalinating plant.
Fig. 3 is a synoptic diagram of the present utility model.
Among Fig. 3: the 1st, well heater, the 2nd, first evaporator, the 3rd, first step fresh water jar, the 4th, first step condenser, the 5th, second stage vaporizer, the 6th, second stage fresh water jar, the 7th, second stage condenser, the 8th, third evaporator, the 9th, the last step vaporizer, the 10th, last step fresh water jar, the 11st, the last step condenser, the 12nd, the water cooler of last step condenser, the 13rd, be the flow control valve of first evaporator moisturizing, the 14th, first evaporator is to the flow control valve of second stage vaporizer moisturizing, the 15th, first step fresh water jar take out the fresh-water flow variable valve, the 16th, second stage vaporizer is to the flow control valve of third evaporator moisturizing, the 17th, second stage fresh water jar take out the fresh-water flow variable valve, the 18th, the flow control valve of the discharge concentrated seawater of last step vaporizer, the 19th, last step fresh water jar take out the fresh-water flow variable valve, the 20th, the fresh water afterheat heat exchanger.
(5) embodiment
Fig. 3 is an embodiment of the present utility model.
At first, first evaporator (2) is seethed with excitement by well heater (1) heating, after the steam that produces enters first step condenser (4) by pipeline, being condensed into distilled water after the cooled with seawater in the second stage vaporizer (5) enters first step fresh-water tank (3), the Absorption by Sea Water latent heat of condensation in the second stage vaporizer (5) is until boiling simultaneously, the steam that produces flows into second stage condenser (7), condensed after the cooled with seawater in the third stage vacuum-evaporator (8), water of condensation flows in the second stage fresh-water tank (6).Third stage vacuum-evaporator is heated boiling.By that analogy, the subsequent stages vacuum distilling apparatus is successively by the previous stage ebuillition of heated.The steam that last step vaporizer (9) boiling produces enters the condenser (11) of last step, and condenses after the cooled with seawater in the device that is cooled (12), and agglomerative distilled water enters last step fresh-water tank (10).
First step fresh-water tank (3), second stage fresh-water tank (6), the fresh water in last step fresh-water tank (19) and other fresh-water tanks at different levels pass through flow control valve (15,17 and 19 etc.) respectively and enter seawater in fresh water afterheat heat exchanger (20) heating heat exchanger.And normal temperature seawater at first enters water cooler (12), with the heat of condensation that absorption last step vacuum distillation plant condenser (11) produces, and the fresh water afterheat heat exchanger (20) of flowing through again, the fresh water that is produced by vacuum distilling heats, thereby has realized fresh water waste heat recovery process.
Seawater process by fresh water afterheat heat exchanger (20) heating enters first step vacuum-evaporator (2) for the flow control valve (13) of first evaporator moisturizing, and the seawater in the first evaporator is by for the flow control valve (14) of second stage vaporizer moisturizing be second stage vaporizer (5) moisturizing, and the interior seawater of second stage vaporizer (5) pass through for the flow control valve (16) of third evaporator moisturizing be third evaporator (8) moisturizing; And the like, the vaporizer of previous stage is back one-level vaporizer moisturizing by flow control valve respectively.Because the pressure in the previous stage vaporizer is higher than the pressure of back one-level, so the moisturizing process only needs suitably to regulate flow control valve and can finish automatically.In the moisturizing process, because the boiling temperature of previous stage vaporizer is higher than back one-level vaporizer, therefore after the seawater of previous stage vaporizer enters the next stage vaporizer, at first some seawater generation flash distillation, then with this grade vaporizer in together explosive evaporatoin of seawater, the steam of generation enters condensation in the condenser of this grade.
Whole water replanishing device relies on flow control valve that the seawater liquid level in the vaporizers at different levels is remained on the appropriate location.The steam that vaporizers at different levels produce is at first removed sea water drops by the scum dredger of this grade, then enters condenser.
18 is flow control valves that concentrated seawater is discharged among Fig. 3, by this flow control valve concentrated seawater is extracted out.Control concentrated seawater delivery flow variable valve (18) can be controlled the flow of taking concentrated seawater away, thereby controls the concentration of seawater in this grade vaporizer; The flow of taking concentrated seawater away is big more, and the concentration of concentrated seawater is low more, and the concentration of the more little concentrated seawater of flow is high more.Suitably dominant discharge variable valve (18) can be controlled at the concentration interval that helps improving vaporization efficiency and fresh water quality most with the concentration of discharging concentrated seawater.
In the such scheme, the thermal source of well heater (1) can be the waste heat of chemical plant or power plant, also can be the hot water that solar energy system produces, also directly electricity consumption under special circumstances, coal or Sweet natural gas heating.
Claims (1)
1. multilevel vacuum distilling sea water desalinating plant, by some groups of placed in-line vacuum distilling apparatuses, well heater (1), water cooler (12), and fresh water afterheat heat exchanger (20) is formed, every group of vacuum distilling apparatus is made up of vaporizer (2,5,9), condenser (4,7,11), fresh-water tank (3,6,10), it is characterized in that: the condenser of previous stage (4) is immersed in the seawater of back one-level vaporizer (5), and previous stage vaporizer (2) links to each other with the vaporizer (5) of next stage through flow control valve (14).
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009202702592U CN201587871U (en) | 2009-11-27 | 2009-11-27 | Multi-stage vacuum distillation seawater desalination device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009202702592U CN201587871U (en) | 2009-11-27 | 2009-11-27 | Multi-stage vacuum distillation seawater desalination device |
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| CN201587871U true CN201587871U (en) | 2010-09-22 |
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| CN2009202702592U Expired - Lifetime CN201587871U (en) | 2009-11-27 | 2009-11-27 | Multi-stage vacuum distillation seawater desalination device |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102205993A (en) * | 2011-03-18 | 2011-10-05 | 清华大学 | Adverse current closed type multistage seawater desalination system and method |
| CN102285702A (en) * | 2011-05-31 | 2011-12-21 | 于庆坤 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN102718276A (en) * | 2012-07-12 | 2012-10-10 | 众和海水淡化工程有限公司 | Efficient low-temperature multi-effect evaporation sea water desalting plant |
| CN102976421A (en) * | 2012-11-22 | 2013-03-20 | 中国神华能源股份有限公司 | Sea water desalination system |
| CN104828995A (en) * | 2015-05-20 | 2015-08-12 | 中冶东方工程技术有限公司 | Treatment method of ferrous waste hydrochloric acid |
| CN104909418A (en) * | 2014-03-10 | 2015-09-16 | 张传征 | Wide-temperature-zone total heat recovery seawater desalination/distillation apparatus |
| CN105271458A (en) * | 2014-06-09 | 2016-01-27 | 程长青 | Multi-effect vacuum boiling type sea water desalinization apparatus |
| CN110697816A (en) * | 2019-10-24 | 2020-01-17 | 上海发电设备成套设计研究院有限责任公司 | A compact distillation apparatus and system and its application |
-
2009
- 2009-11-27 CN CN2009202702592U patent/CN201587871U/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102205993A (en) * | 2011-03-18 | 2011-10-05 | 清华大学 | Adverse current closed type multistage seawater desalination system and method |
| CN102205993B (en) * | 2011-03-18 | 2013-02-13 | 清华大学 | Adverse current closed type multistage seawater desalination system and method |
| CN102285702A (en) * | 2011-05-31 | 2011-12-21 | 于庆坤 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN102285702B (en) * | 2011-05-31 | 2014-07-16 | 烟台豪杰能源科技有限公司 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN102718276A (en) * | 2012-07-12 | 2012-10-10 | 众和海水淡化工程有限公司 | Efficient low-temperature multi-effect evaporation sea water desalting plant |
| CN102718276B (en) * | 2012-07-12 | 2014-01-08 | 众和海水淡化工程有限公司 | Efficient low-temperature multi-effect evaporation sea water desalting plant |
| CN102976421A (en) * | 2012-11-22 | 2013-03-20 | 中国神华能源股份有限公司 | Sea water desalination system |
| CN102976421B (en) * | 2012-11-22 | 2014-07-09 | 中国神华能源股份有限公司 | Sea water desalination system |
| CN104909418A (en) * | 2014-03-10 | 2015-09-16 | 张传征 | Wide-temperature-zone total heat recovery seawater desalination/distillation apparatus |
| CN105271458A (en) * | 2014-06-09 | 2016-01-27 | 程长青 | Multi-effect vacuum boiling type sea water desalinization apparatus |
| CN104828995A (en) * | 2015-05-20 | 2015-08-12 | 中冶东方工程技术有限公司 | Treatment method of ferrous waste hydrochloric acid |
| CN110697816A (en) * | 2019-10-24 | 2020-01-17 | 上海发电设备成套设计研究院有限责任公司 | A compact distillation apparatus and system and its application |
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Granted publication date: 20100922 |