CN106698563A - Multi-effect membrane distillation seawater desalination system based on mechanical compression - Google Patents
Multi-effect membrane distillation seawater desalination system based on mechanical compression Download PDFInfo
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- CN106698563A CN106698563A CN201710056217.8A CN201710056217A CN106698563A CN 106698563 A CN106698563 A CN 106698563A CN 201710056217 A CN201710056217 A CN 201710056217A CN 106698563 A CN106698563 A CN 106698563A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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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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- 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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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a multi-effect membrane distillation seawater desalination system based on mechanical compression. The multi-effect membrane distillation seawater desalination system based on the mechanical compression comprises a plurality of serially-connected vacuum membrane distillation assemblies and heat exchange assemblies, a plurality of serially-connected concentrated water flash distillation tanks, a plurality of serially-connected fresh water flash distillation tanks, a mechanical steam compressor and a vacuumizing system, wherein the serially-connected vacuum membrane distillation assemblies and the heat exchange assemblies form multi-effect distillation in the conventional distillation sense; the serially-connected concentrated water flash distillation tanks receive concentrated seawater after membrane distillation and perform stage-by-stage flash distillation, and flash distillation steam is used as heating steam corresponding to each-effect material liquids; the serially-connected fresh water flash distillation tanks receive fresh water produced during the membrane distillation and perform stage-by-stage flash distillation, and flash distillation steam is used as heating steam corresponding to each-effect material liquids; the mechanical steam compressor raises the temperature and the pressure of secondary steam produced by the last-effect membrane distillation assembly through consumption of electric energy, and provides heating steam for the first-effect heat exchange assembly. The multi-effect membrane distillation seawater desalination system based on the mechanical compression couples a multi-effect membrane distillation process and a multi-stage flash distillation process, pumps the last-effect secondary steam through the mechanical steam compressor, and recycles the last-effect secondary steam after quality improvement to achieve gradient utilization of energy and two-way concentration of the material liquid, so that consumption of cooling water is not required, the heat efficiency is high, the water making ratio is high, the concentrating ratio is high, and the adaptability is high.
Description
Technical field
The invention belongs to UF membrane and field of sea water desalting technology, it is related to a kind of multiple-effect Membrane Materials sea based on mechanical compress
Water desalination system.
Background technology
With expanding economy and the increase of population, the mankind are continuously increased to the demand of water resource, along with the presence of to water
There is different degrees of water shortage problem in the unreasonable exploitation and utilization of resource, many countries and regions, and the whole world is faced with increasingly
Serious water resources crisis.
Desalinization is to realize the increment technique of increasing income that water resource is utilized, and can increase fresh water total amount, and by space-time and
Climatic effect, can ensure the stable water supply such as coastal Drinking Water for Residents and Industrial Boiler moisturizing.Desalinization, it is de- also known as seawater
Salt, is the technology and process for separating salt and water in seawater, its essence is " changing water source with the energy ".At present, commercial desalinization
Technology mainly has multi-effect distilling (MED), multistage flash evaporation (MSF), mechanical compress distillation (MVR), counter-infiltration (RO) etc..MED、MSF
Belong to hot method desalination technology with MVR, its technical advantage is the cascade utilization or compression recycling for being capable of achieving energy, but is also deposited
Big in equipment investment, material requirement is high, the low problem of loading density.RO belongs to membrane separation technique, and it has scaleable, initial
The advantages of investment small, wide adaptation range, but there is also, membrane material maintenance cost extremely sensitive to feed liquid ocean temperature and salinity
It is high, the shortcomings of need operation with high pressure.
Membrane Materials (MD) are the membrane separating process that membrane technology is combined with still-process.The technology with dewatering microporous film be situated between
Matter, in the presence of the steam pressure difference of film both sides, volatile component passes through fenestra in vapour form in feed liquid, so as to realize liquid matter point
From.Therefore, the characteristics of film distillation technology is the characteristics of organically combining distillation and membrane process, it is existing normal during Membrane Materials
Evaporation, mass transfer, condensation process in rule distillation, have separate substance to spread the membrane separating process through film, so that the technology again
With separative efficiency is high, operating condition gentle, to the low advantage of mechanical property requirements of film and material liquid interphase interaction and film,
There is preferable application prospect in desalinization and field of industrial waste water treatment.According to the difference of volatile component condensing mode, film
Distillation can be divided into direct contact membrane distillation (DCMD), gap field orientation (AGMD), sweep gas membrane disillation (SGMD) and decompression
Four kinds of modes of Membrane Materials (VMD).Wherein VMD has the advantages that flux is big, heat loss is small, and application prospect is the most wide.
Membrane Materials are that momentum, heat and quality intercouple while the process of transmission.Pass through hydrophobicity during Membrane Materials
The heat transfer of perforated membrane and mass transfer are carried out simultaneously.Mass transfer occurs by fenestra, and heat transfer is produced by film matrix and fenestra
It is raw.Heat transfer both included with the latent heat that is transmitted by the steam or gas flux of fenestra, also including by membrane material and filling
There is the sensible heat of the fenestra transmission of gas.Therefore, the Membrane Materials thermal efficiency is low, high energy consumption, and this is also the pass for limiting its industrial applications
One of key problem.
Patent of invention CN101797479B discloses a kind of side that vacuum membrane distillation is carried out using live (open) steam compressing hot pump
Method and device.It is mainly the indirect steam that Membrane Materials generation is lifted by vapour compression machine, the indirect steam after increasing temperature and pressure
As the heating steam of Membrane Materials feed liquid, to realize the recycling of the latent heat of vaporization.But the invention uses single-action Membrane Materials, vapour
Changing latent heat does not carry out cascade utilization, and water generation ratio is low；And feed liquid is only just directly discharged by a Membrane Materials in the invention, is caused
Fresh-water recovery rate is low and pump work consumes increase.
General Electric (U.S.A.) patent of invention CN103080013B discloses a kind of steam compressed Membrane Materials system and method.Its
The latent heat of vaporization that Membrane Materials produce steam mainly is reclaimed by setting Membrane Materials module, and by vapour compression machine by Membrane Materials
The high temperature side of Membrane Materials module is transported to after the cold steam lifting quality of module low temperature side as heating steam.The patent of invention
In, the pressure in " repeat to " that be made up of Membrane Materials film and heat transfer film is uncontrollable, that is, between " repeat to "
Pressure differential be uncontrollable, with accumulation of the incondensable gas in " repeat to ", the pressure in " repeat to " can be gradually
Raise, and the patent does not consider the discharge of fixed gas in " repeat to " and the barometric gradient regulation and control between " repeat to ", this can be caused
Make the steam compressed Membrane Materials system cannot stable operation.Additionally, the patent of invention realizes the recovery profit of the Membrane Materials latent heat of vaporization
With, but the sensible heat of output fluid does not carry out cascade utilization, and part sensible heat is disposably tightly passed into discrepancy by heat exchanger
Raw material stream, from for the angle of multistage Membrane Materials heat balance, this can cause the system thermal efficiency to reduce.
Patent of invention CN102371120B is related to multi-stag pressure reducing film distillation assembly unit device and its Membrane Materials, the device
It is made up of the membrane module and heat-exchanging component of multiple series connection, the steam that so previous membrane module is produced can be used for next film
The heating of component feed liquid, so that the recycling by the latent heat of vaporization improves the thermal efficiency.The patent of invention is needed with set terminal
Condenser is used to cool down the indirect steam of final stage membrane component generation, and needs to consume substantial amounts of cooling water, cooling water heat
Amount loss can reduce system thermal efficiency.
The content of the invention
The present invention seeks to overcome deficiency of the prior art, there is provided a kind of technique is advanced, the thermal efficiency is high, water generation ratio is big,
Cocnentration factor is high, the adaptable multiple-effect film distilling seawater desalination system based on mechanical compress.
Technical scheme is summarized as follows：
A kind of multiple-effect film distilling seawater desalination system based on mechanical compress, including Mechanical Vapor Compression 17, concentrated water drainage
Pump 21 is put, vavuum pump 24, product water pump 22, seawater feed pump 23, N number of membrane module, N number of fresh water flash tank, N number of material liquid tank is N number of
Heat-exchanging component, N-1 concentrated water flash tank, N number of feed pump, also including concentrated water heat exchanger 15 and fresh water heat exchanger 16, mechanical vapour
The outlet of compressor 17 is connected by pipeline with the steam inlet of first heat-exchanging component 7, the condensation water out of first heat-exchanging component 7
After being connected in series to last fresh water flash tank 12 successively from first fresh water flash tank 10 by pipeline, then with product water pump 22
Import is connected；The outlet of product water pump 22 is connected by pipeline with fresh water heat exchanger 16, and fresh water is provided with fresh water heat exchanger 16
Efferent duct；
The outlet of seawater feed pump 23 is divided into two pipelines, and the liquor inlet with concentrated water heat exchanger 15 is connected all the way, another
Road is connected with the liquor inlet of fresh water heat exchanger 16, and the material liquid outlet of concentrated water heat exchanger 15 is by pipeline and fresh water heat exchanger 16
Material liquid outlet is connected after converging by pipeline and is connected with a last material liquid tank 6；
The last material liquid outlet of the bottom of material liquid tank 6 by pipeline successively with last feed pump 20, end heat-exchanging component 9 and end
The liquor inlet connection of the bottom of individual membrane module 3, the material liquid outlet at the top of end membrane module 3 is divided into two pipelines, all the way with end
The top of material liquid tank 6 connection, another road connects with penultimate adjacent material liquid tank 5, repeats the connected mode of this section to first feed liquid
Tank 4；
The material liquid outlet of the bottom of first material liquid tank 4 by pipeline successively with first feed pump 18, first heat-exchanging component 7 and head
The liquor inlet connection of the bottom of individual membrane module 1, the material liquid outlet at the top of first membrane module 1 is divided into two pipelines, leads up to pipe
Road is connected with the top of first material liquid tank 4, separately leads up to pipeline and is flashed to last concentrated water successively from first concentrated water flash tank 13
After tank 14 is connected in series, then it is connected with the import of concentrated water discharge pump 21；The outlet of concentrated water discharge pump 21 is changed by pipeline with concentrated water
Hot device 15 is connected, and concentrated seawater delivery pipe is provided with concentrated water heat exchanger 15；
The steam (vapor) outlet of first membrane module 1 by the fixed gas of pipeline and first heat-exchanging component 7 export the pipeline being connected with
And first fresh water flash tank 10 steam (vapor) outlet connection pipeline converge after be connected with the steam inlet of secondary heat-exchanging component (8)；
Pipeline that secondary steam (vapor) outlet of membrane module 2 is connected by pipeline with the steam (vapor) outlet of first concentrated water flash tank 13,
The pipeline of the secondary steam (vapor) outlet connection of the pipeline and a time fresh water flash tank 11 of the fixed gas outlet connection of heat-exchanging component 8 converges
The steam inlet with next heat-exchanging component is connected afterwards；Repeat the connected mode of this section to the steam inlet of last individual heat-exchanging component 9
Connection；
Pipeline that the last steam (vapor) outlet of membrane module 3 is connected by the steam (vapor) outlet of the individual concentrated water flash tank 14 in pipeline and end and
The jetting steam caused entrance that the pipeline of the last steam (vapor) outlet connection of fresh water flash tank 12 converges rear and Mechanical Vapor Compression 17 connects
Connect, the fixed gas outlet of end heat-exchanging component 9 is connected by pipeline with vavuum pump 24；
Secondary heat-exchanging component 8 is self-corresponding with each respectively by pipeline to each condensation water out of last heat-exchanging component 9
Fresh water flash tank is connected, and N is 2-15.
Membrane module is preferred：Hollow fiber form membrane component, tubular type membrane component, rolling membrane component or plate and frame
Membrane component.
Heat-exchanging component is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Concentrated water heat exchanger is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Fresh water heat exchanger is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Mechanical Vapor Compression is preferred：Centrifugal compressor, lobed rotor compressor or helical-lobe compressor.
Advantages of the present invention：
(1) system of the invention is utilized, the indirect steam that previous effect Membrane Materials are produced is used as the latter heating for imitating Membrane Materials
Steam, so as to realize the cascade utilization of the Membrane Materials latent heat of vaporization, has effectively reclaimed the latent heat of vaporization and has improve system thermal efficiency
And water generation ratio.
(2) present invention can be such that the high temperature concentrated seawater and product water of the discharge of multiple-effect Membrane Materials is dodged step by step in each flash tank
Steam, flash-off steam is used for the feed liquid heating of seawater of each effect Membrane Materials of correspondence, it is achieved thereby that the sensible heat of output concentrated water and fresh water
Cascade utilization is concentrated with the round trip of feed liquid, further increases system thermal efficiency and water generation ratio.
(3) Mechanical Vapor Compression that system is set, under conditions of supply of electric power is only needed to, end effect Membrane Materials is produced
Indirect steam increasing temperature and pressure, as the first heat source for imitating Membrane Materials, so, the latent heat of vaporization of indirect steam after lifting quality
It is generally reused many times by multiple-effect Membrane Materials process, relative to the technique of mechanical vapour compression machine, system water generation ratio is improved
Several times.
(4) system of the invention can make seawater feeding manner using " respectively adverse current feeding+following current between effect independent loops+effect
The technological process of flash distillation step by step ", " respectively imitating independent loops " can respectively imitate the cocnentration factor of Membrane Materials with precise control, in non crystallized bar
Under part, highest feed liquid concentration rate is realized；" adverse current feeding between effect " makes feed liquid seawater be gradually heated up from low temperature to high temperature, while
Membrane Materials are carried out by effect, the small different transfer of heat of cold fluid and hot fluid is capable of achieving, heat-economy is more preferable；" following current is flashed step by step " can make defeated
Go out concentrated water and fresh water is flashed step by step between effect in the presence of pressure differential, flash-off steam is heated for Membrane Materials feed liquid, is further carried
System thermal efficiency high.
(5) the system belongs to the integrated innovation of the technical process such as multi-effect distilling, multistage flash evaporation, both vapor compression recycling, tool
Have the advantages that technique is advanced, the thermal efficiency is high, cocnentration factor is big, strong adaptability, and heating steam and cooling extraneous need not be provided
Water a, consumption electric power substantially increases system application, than if being applied to space urine zero discharge treatment, remote island
Supply water etc..
Brief description of the drawings
Fig. 1 is a kind of multiple-effect film distilling seawater desalination system schematic diagram based on mechanical compress.
Specific embodiment
With reference to Fig. 1, the present invention is further illustrated so that N is equal to 3 as an example.The description below is in order that this area
Technical staff better understood when the present invention, but the present invention do not imposed any restrictions.
A kind of multiple-effect film distilling seawater desalination system based on mechanical compress, including Mechanical Vapor Compression 17, concentrated water drainage
Put pump 21, vavuum pump 24, product water pump 22,23,3 membrane modules of seawater feed pump, 3 fresh water flash tanks, 3 material liquid tanks, 3
Heat-exchanging component, 2 concentrated water flash tanks, 3 feed pumps, also including concentrated water heat exchanger 15 and fresh water heat exchanger 16, mechanical vapour pressure
The outlet of contracting machine 17 is connected by pipeline with the steam inlet of first heat-exchanging component 7, and the condensation water out of first heat-exchanging component 7 leads to
Cross pipeline and a time fresh water flash tank 11 is passed sequentially through from first fresh water flash tank 10, be connected in series to last fresh water flash tank 12
Afterwards, then with the import of product water pump 22 it is connected；The outlet of product water pump 22 is connected by pipeline with fresh water heat exchanger 16, and fresh water is changed
Fresh water efferent duct is provided with hot device 16；
The outlet of seawater feed pump 23 is divided into two pipelines, and the liquor inlet with concentrated water heat exchanger 15 is connected all the way, another
Road is connected with the liquor inlet of fresh water heat exchanger 16, and the material liquid outlet of concentrated water heat exchanger 15 is by pipeline and fresh water heat exchanger 16
Material liquid outlet is connected after converging by pipeline and is connected with a last material liquid tank 6；
The last material liquid outlet of the bottom of material liquid tank 6 by pipeline successively with last feed pump 20, end heat-exchanging component 9 and end
The liquor inlet connection of the bottom of individual membrane module 3, the material liquid outlet at the top of end membrane module 3 is divided into two pipelines, all the way with end
The connection of the top of material liquid tank 6, another road connects with penultimate adjacent material liquid tank 5；
Penultimate material liquid outlet of the bottom of material liquid tank 5 by pipeline successively with penultimate feed pump 19, penultimate heat exchange group
Part 8 and the penultimate liquor inlet connection of the bottom of membrane module 2, the material liquid outlet at the penultimate top of membrane module 2 are divided into two pipelines,
It is connected with the penultimate top of material liquid tank 5 all the way, another road connects with adjacent first material liquid tank 4；
The material liquid outlet of the bottom of first material liquid tank 4 by pipeline successively with first feed pump 18, first heat-exchanging component 7 and head
The liquor inlet connection of the bottom of individual membrane module 1, the material liquid outlet at the top of first membrane module 1 is divided into two pipelines, leads up to pipe
Road is connected with the top of first material liquid tank 4, separately leads up to pipeline from first concentrated water flash tank 13 to last concentrated water flash tank 14
After being connected in series, then it is connected with the import of concentrated water discharge pump 21；The outlet of concentrated water discharge pump 21 is by pipeline and concentrated water heat exchanger
15 connections, are provided with concentrated seawater delivery pipe on concentrated water heat exchanger 15；
The steam (vapor) outlet of first membrane module 1 by the fixed gas of pipeline and first heat-exchanging component 7 export the pipeline being connected with
And first fresh water flash tank 10 steam (vapor) outlet connection pipeline converge after be connected with the steam inlet of secondary heat-exchanging component 8；
Pipeline that secondary steam (vapor) outlet of membrane module 2 is connected by pipeline with the steam (vapor) outlet of first concentrated water flash tank 13,
The pipeline of the secondary steam (vapor) outlet connection of the pipeline and a time fresh water flash tank 11 of the fixed gas outlet connection of heat-exchanging component 8 converges
The steam inlet connection of end heat-exchanging component 9 afterwards；
Pipeline that the last steam (vapor) outlet of membrane module 3 is connected by the steam (vapor) outlet of the individual concentrated water flash tank 14 in pipeline and end and
The jetting steam caused entrance that the pipeline of the last steam (vapor) outlet connection of fresh water flash tank 12 converges rear and Mechanical Vapor Compression 17 connects
Connect；The fixed gas outlet of last heat-exchanging component 9 is connected by pipeline with vavuum pump 24；
The secondary condensation water out of heat-exchanging component 8 is connected by pipeline with secondary fresh water flash tank 11, end heat-exchanging component 9
Condensation water out be connected by the individual fresh water flash tank 12 in pipeline and end.
N can also select 2,3,4,5,6,7,8,9,10,11,12,13,14,15
Membrane module is preferred：Hollow fiber form membrane component, tubular type membrane component, rolling membrane component or plate and frame
Membrane component.
Heat-exchanging component is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Concentrated water heat exchanger is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Fresh water heat exchanger is preferred：Shell-and-tube heat exchanger or plate type heat exchanger.
Mechanical Vapor Compression is preferred：Centrifugal compressor, lobed rotor compressor or helical-lobe compressor.
Embodiment 1
Desalination process flow is carried out using said system：
First, feed liquid seawater is divided into two strands after seawater feed pump 23, and one enters the tube side of concentrated water heat exchanger 15 with row
Concentrated seawater heat exchange is put, another strand enters the tube side of fresh water heat exchanger 16 and exchanged heat with fresh water, and the feed liquid seawater after two bursts of heat exchange heat up converges
Enter the feed liquid of last 6. seawater material liquid tank of material liquid tank 6 bottom outflow after conjunction through last feed pump 20 into end heat-exchanging component 9
Cold side, condensation is from secondary membrane module 2, first concentrated water flash tank 13 and the secondary steaming of the higher temperature of the generation of fresh water flash tank 11
Vapour and from the steam entrained by the secondary fixed gas of heat-exchanging component 8, while feed liquid itself is heated to temperature higher, so
Feed liquid enters in the hollow-fibre membrane of end membrane module 3 afterwards, and Membrane Materials are carried out under the driving of the cross-film temperature difference, in last membrane module
Feed liquid after 3 completion Membrane Materials is divided into two parts：A part returns to end material liquid tank 6, and last feed pump is then passed sequentially through again
20th, end heat-exchanging component 9, end membrane module 3, are so repeated the Membrane Materials process of feed liquid, until reaching required feed liquid
Cocnentration factor；Another part enters penultimate material liquid tank 5.The penultimate feed liquid of the bottom of material liquid tank 5 outflow is through penultimate feed pump 19
Into the secondary cold side of heat-exchanging component 8, the steaming of the higher temperature that condensation is produced from first membrane module 1, first fresh water flash tank 10
Steam entrained by the fixed gas of vapour and first heat-exchanging component 7, while feed liquid itself is heated to temperature higher, then expects
Liquid enters in time hollow-fibre membrane of a membrane module 2, and Membrane Materials are carried out under the driving of the cross-film temperature difference；Film is completed in membrane module 2
Feed liquid after distillation is divided into two parts：A part return penultimate material liquid tank 5, then pass sequentially through again penultimate feed pump 19,
Secondary heat-exchanging component 8, secondary membrane module 2, are so repeated the Membrane Materials process of feed liquid, until the feed liquid concentration needed for reaching
Than；Another part enters first material liquid tank 4；The feed liquid of the bottom of first material liquid tank 4 outflow is changed through first feed pump 18 into first
The cold side of hot component 7, condensation from Mechanical Vapor Compression 17 provide heating steam, while feed liquid itself be heated to it is higher
Temperature, then feed liquid enter first membrane module 1 hollow-fibre membrane in, Membrane Materials are carried out under the driving of the cross-film temperature difference；Feed liquid
Seawater is raised with multiple-effect Membrane Materials process, temperature by effect, and concentration increases by effect.
The concentrated seawater (temperature highest) for completing Membrane Materials in first membrane module 1 is divided into two parts：A part returns to first material
Flow container 4, then passes sequentially through first feed pump 18, first heat-exchanging component 7, first membrane module 1 again, and feed liquid is so repeated
Membrane Materials process, until reaching required feed liquid cocnentration factor；Another part is flashed into first concentrated water flash tank 13, is flashed off
Steam enters the end hot side of heat-exchanging component 9 between effect in the presence of barometric gradient, heat the feed liquid seawater of cold side；Discharged after flash distillation
Concentrated seawater enter end concentrated water flash tank 14 and flash, the steam for flashing off enters compressor 17；In last concentrated water flash tank 14
The concentrated seawater (temperature is minimum, and concentration is maximum) discharged after flash distillation is delivered to concentrated water heat exchanger 15 with charging sea by concentrated water discharge pump 21
Discharged after water heat exchange.
The fresh water that the condensation of the hot side of first heat-exchanging component 7 is produced, flashes, the steam for flashing off into first fresh water flash tank 10
Enter a time hot side of heat-exchanging component 8 in the presence of barometric gradient between effect, heat cold side feed liquid seawater；First fresh water flash tank 10
After the fresh water that fresh water after flash distillation is produced with the secondary hot side of heat-exchanging component 8 condensation converges, flashed into secondary fresh water flash tank 11,
The steam for flashing off enters the end hot side of heat-exchanging component 9 between effect in the presence of barometric gradient, heat the feed liquid seawater of cold side；It is secondary
It is light into last after fresh water after the individual flash distillation of fresh water flash tank 11 converges with the fresh water of the end hot side condensation generation of heat-exchanging component 9
Water flash tank 12 is flashed, and the steam for flashing off enters compressor 17, and the fresh water after flash distillation is delivered to fresh water and changes by product water pump 22
Exported after hot device 16 and charging seawater to make heat exchange.
In the presence of Mechanical Vapor Compression 17, from last membrane module 3, the individual concentrated water flash tank 14 in end and end fresh water
The steam that flash tank 12 is produced is volleyed, is compressed the initial heating steam collectively as first heat-exchanging component 7 after heating up.
In the presence of vavuum pump 24, fresh water flash tank 10,11,12, heat-exchanging component 7,8,9, membrane module 1,2,3, concentrated water
Flash tank 13,14, keeps negative pressure state；The vacuum of each membrane module and heat-exchanging component is by the regulating valve in vacuum-pumping pipeline
Control, the mode that vacuumizes of each heat-exchanging component is series connection pumping, i.e. hot side of the fixed gas successively from heat-exchanging component 7,8,9 is passed through,
Finally extracted out by vavuum pump 24.
Membrane module, heat-exchanging component, material liquid tank, membrane module feed pump are sequentially connected by pipeline, form Conventional espresso meaning
On " effect " Membrane Materials.
Described " effect " Membrane Materials, membrane module has N number of membrane module composition in parallel.
Multiple " effect " Membrane Materials are sequentially connected in series by pipeline, form multiple-effect Membrane Materials, and steam is produced for Membrane Materials
The latent heat of vaporization recycling step by step.
Concentrated water flash tank, is sequentially connected in series by pipeline, forms concentrated water multistage flash evaporation, for Membrane Materials discharge concentrated water
The recycling step by step of sensible heat.
Fresh water flash tank, is sequentially connected in series by pipeline, forms fresh water multistage flash evaporation, for Membrane Materials output fresh water
The recycling step by step of sensible heat.
Discharge concentrated seawater transfers heat to charging seawater with output fresh water by heat-exchanging component, further recycles system
The heat of system discharge fluid.
Claims (6)
1. a kind of multiple-effect film distilling seawater desalination system based on mechanical compress, including Mechanical Vapor Compression (17), concentrated water drainage
Put pump (21), vavuum pump (24), product water pump (22), seawater feed pump (23), N number of membrane module, N number of fresh water flash tank, N number of material
Flow container, N number of heat-exchanging component, N-1 concentrated water flash tank, N number of feed pump, it is characterized in that also including concentrated water heat exchanger (15) and fresh water
Heat exchanger (16), the outlet of Mechanical Vapor Compression (17) is connected by pipeline with the steam inlet of first heat-exchanging component (7), first
The condensation water out of individual heat-exchanging component (7) passes through pipeline from first fresh water flash tank (10) successively to last fresh water flash tank
(12) after being connected in series, then it is connected with the import of product water pump (22)；The outlet of product water pump (22) is changed by pipeline with fresh water
Hot device (16) connection, fresh water heat exchanger is provided with fresh water efferent duct on (16)；
The outlet of seawater feed pump (23) is divided into two pipelines, and the liquor inlet with concentrated water heat exchanger (15) is connected all the way, another
Road is connected with the liquor inlet of fresh water heat exchanger (16), and the material liquid outlet of concentrated water heat exchanger (15) passes through pipeline and fresh water heat exchanger
(16) material liquid outlet is connected after converging by pipeline and is connected with a last material liquid tank (6)；
The last material liquid outlet of material liquid tank (6) bottom by pipeline successively with last feed pump (20), end heat-exchanging component (9) and
The last liquor inlet connection of membrane module (3) bottom, the material liquid outlet at the top of the membrane module (3) of end is divided into two pipelines, all the way
It is connected with last material liquid tank (6) top, another road connects with penultimate adjacent material liquid tank (5), repeats the connected mode of this section
To first material liquid tank (4)；
The material liquid outlet of first material liquid tank (4) bottom by pipeline successively with first feed pump (18), first heat-exchanging component (7) and
The liquor inlet connection of first membrane module (1) bottom, the material liquid outlet at the top of first membrane module (1) is divided into two pipelines, all the way
It is connected with first material liquid tank (4) top by pipeline, separately leads up to pipeline from first concentrated water flash tank (13) successively to end
After individual concentrated water flash tank (14) is connected in series, then it is connected with the import of concentrated water discharge pump (21)；The outlet of concentrated water discharge pump (21)
It is connected with concentrated water heat exchanger (15) by pipeline, concentrated water heat exchanger is provided with concentrated seawater delivery pipe on (15)；
The steam (vapor) outlet of first membrane module (1) by the fixed gas of pipeline and first heat-exchanging component (7) export the pipeline being connected with
And the pipeline of the steam (vapor) outlet connection of first fresh water flash tank (10) converge after connect with the steam inlet of secondary heat-exchanging component (8)
Connect；
Pipeline that secondary steam (vapor) outlet of membrane module (2) is connected by pipeline with the steam (vapor) outlet of first concentrated water flash tank (13),
The secondary pipeline of the steam (vapor) outlet connection of the pipeline and time fresh water flash tank (11) of the fixed gas outlet connection of heat-exchanging component (8)
Steam inlet after converging with next heat-exchanging component is connected；Repeat the connected mode of this section to the steaming of last individual heat-exchanging component (9)
Vapor inlet is connected；
Pipeline that the last steam (vapor) outlet of membrane module (3) is connected by the steam (vapor) outlet of individual concentrated water flash tank (14) in pipeline and end and
The pipeline of the last steam (vapor) outlet connection of fresh water flash tank (12) converge after with Mechanical Vapor Compression (17) it is jetting steam caused enter
Mouth connection, the fixed gas outlet of end heat-exchanging component (9) is connected by pipeline with vavuum pump 24；
Secondary heat-exchanging component (8) is self-corresponding with each respectively by pipeline to each condensation water out of end heat-exchanging component (9)
Fresh water flash tank is connected, and N is 2-15.
2. the multiple-effect film distilling seawater desalination system based on mechanical compress according to claim 1, it is characterised in that described
Membrane module is hollow fiber form membrane component, tubular type membrane component, rolling membrane component or plate and frame membrane component.
3. the multiple-effect film distilling seawater desalination system based on mechanical compress according to claim 1, it is characterised in that described
Heat-exchanging component is shell-and-tube heat exchanger or plate type heat exchanger.
4. the multiple-effect film distilling seawater desalination system based on mechanical compress according to claim 1, it is characterised in that described
Concentrated water heat exchanger is shell-and-tube heat exchanger or plate type heat exchanger.
5. the multiple-effect film distilling seawater desalination system based on mechanical compress according to claim 1, it is characterised in that described
Fresh water heat exchanger is shell-and-tube heat exchanger or plate type heat exchanger.
6. the multiple-effect film distilling seawater desalination system based on mechanical compress according to claim 1, it is characterised in that described
Mechanical Vapor Compression is centrifugal compressor, lobed rotor compressor or helical-lobe compressor.
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| CN201710056217.8A CN106698563A (en) | 2017-01-25 | 2017-01-25 | Multi-effect membrane distillation seawater desalination system based on mechanical compression |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108176231A (en) * | 2018-03-08 | 2018-06-19 | 中国科学院理化技术研究所 | Vacuum type multi-effect membrane distillation system |
| WO2019066687A1 (en) | 2017-09-29 | 2019-04-04 | King Abdulaziz City For Science And Technology | Combined desalinated water production system |
| WO2019083416A1 (en) | 2017-10-23 | 2019-05-02 | King Abdulaziz City For Science And Technology | Water desalination system |
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| CN1397500A (en) * | 2002-08-09 | 2003-02-19 | 周堃 | Multi-effect distilling process and equipment for desalinating seawater |
| CN103387308A (en) * | 2013-08-13 | 2013-11-13 | 国家海洋局天津海水淡化与综合利用研究所 | Multi-effect membrane distillation-multistage flash evaporation seawater desalination system |
| CN105923675A (en) * | 2016-06-14 | 2016-09-07 | 西安交通大学 | Seawater desalination device with heat-pump evaporation coupled with MED |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1397500A (en) * | 2002-08-09 | 2003-02-19 | 周堃 | Multi-effect distilling process and equipment for desalinating seawater |
| CN103387308A (en) * | 2013-08-13 | 2013-11-13 | 国家海洋局天津海水淡化与综合利用研究所 | Multi-effect membrane distillation-multistage flash evaporation seawater desalination system |
| CN105923675A (en) * | 2016-06-14 | 2016-09-07 | 西安交通大学 | Seawater desalination device with heat-pump evaporation coupled with MED |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2019066687A1 (en) | 2017-09-29 | 2019-04-04 | King Abdulaziz City For Science And Technology | Combined desalinated water production system |
| WO2019083416A1 (en) | 2017-10-23 | 2019-05-02 | King Abdulaziz City For Science And Technology | Water desalination system |
| CN108176231A (en) * | 2018-03-08 | 2018-06-19 | 中国科学院理化技术研究所 | Vacuum type multi-effect membrane distillation system |
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Application publication date: 20170524 |