CN106470753A - The vacuum membrane distillation formula fresh water generator of ship - Google Patents
The vacuum membrane distillation formula fresh water generator of ship Download PDFInfo
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- CN106470753A CN106470753A CN201580035241.2A CN201580035241A CN106470753A CN 106470753 A CN106470753 A CN 106470753A CN 201580035241 A CN201580035241 A CN 201580035241A CN 106470753 A CN106470753 A CN 106470753A
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- Prior art keywords
- vacuum
- water
- ship
- sea water
- fresh water
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-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63J—AUXILIARIES ON VESSELS
- B63J1/00—Arrangements of installations for producing fresh water, e.g. by evaporation and condensation of sea water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/365—Osmotic distillation or osmotic evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/26—Polyalkenes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/26—Polyalkenes
- B01D71/261—Polyethylene
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/26—Polyalkenes
- B01D71/262—Polypropylene
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/30—Polyalkenyl halides
- B01D71/32—Polyalkenyl halides containing fluorine atoms
- B01D71/34—Polyvinylidene fluoride
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/30—Polyalkenyl halides
- B01D71/32—Polyalkenyl halides containing fluorine atoms
- B01D71/36—Polytetrafluoroethene
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/66—Polymers having sulfur in the main chain, with or without nitrogen, oxygen or carbon only
- B01D71/68—Polysulfones; Polyethersulfones
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
-
- 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
-
- 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
-
- 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
-
- 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
Abstract
The vacuum membrane distillation formula fresh water generator that height makes the ship of water efficiency can be compactly realized in offer.Vacuum membrane distillation formula fresh water generator (1) of ship has：Heater (10), it heats to the sea water being taken into ship；Vacuum distilling module (11), it possesses and passes through portion (20), vacuum (21), the hydrophobic porous plasma membrane (22) that heating seawater is separated by portion (20) and vacuum (21) for the heating seawater that flow through by the warmed-up sea water of heater (10) and make from heating seawater that by hydrophobic porous plasma membrane (22) and the steam that flows into vacuum (21) cools down and the cooling end (23) of condensation by the sea water being heated of portion (20)；And water jet (61), it is the decompressing unit making vacuum (21) reduce pressure.Heater (10) utilizes the hot heating seawater of the thermal source of ship.The vacuum (21) that makes water jet (61) reduce pressure for below saturated vapour pressure under heating seawater is by the ocean temperature in portion (20) for the water and more than 0.1atm pressure.
Description
Technical field
The present invention relates to the vacuum membrane distillation formula fresh water generator of ship.
Background technology
For the ship navigating by water in ocean it is ensured that the water such as drinking water and domestic water is extremely important.Therefore, develop
The technology of the fresh water generator for manufacturing fresh water from sea water is carried on ship.In this fresh water generator, exist and utilize evaporator
Sea water by distillation is obtained with the device (with reference to patent documentation 1) of fresh water (way of distillation).In addition, in other fresh water generators, existing
Using film, sea water by distillation is obtained with the device (with reference to patent documentation 2) of fresh water (Membrane Materials method).
Prior art literature
Patent documentation
Patent documentation 1：Japanese Unexamined Patent Publication 2008-289976 publication
Patent documentation 2：Japanese Unexamined Patent Publication 2-9490 publication
Content of the invention
Invent problem to be solved
But, for the fresh water generator based on the above-mentioned way of distillation, in order to suppress the spittle adjoint with processing aqueous phase, need really
Protect distance between evaporation part and condensation part, thus there is evaporator and device becomes the tendency that maximizes.On the other hand, for making
With the fresh water generator of Membrane Materials method, inefficient due to making water, therefore, need higher make outlet capacity in the case of, there is dress
Put the tendency becoming to maximize.
On the other hand, on ship, due to needing to carry the main equipment such as electromotor or electromotor, therefore there is no abundance
Space, therefore it is required that fresh water generator is as compact as possible.
That the application is in view of the above problems and completes it is therefore intended that providing a kind of compact and being capable of height and make water efficiency
Ship vacuum membrane distillation formula fresh water generator.
Means for solving the problem
The vacuum membrane distillation formula fresh water generator comprising a kind of ship in the present invention for reaching above-mentioned purpose, its profit
The heat of the thermal source being had with ship, produces fresh water from the sea water being taken into ship, and wherein, the vacuum diaphragm of this ship is steamed
Evaporate formula fresh water generator to have：Heater, it heats to the sea water being taken into ship；Vacuum distilling module, it possesses：For
The heating seawater being flow through by the sea water after described heating devices heat passes through portion；Vacuum；By described heating seawater pass through portion and
The hydrophobic porous plasma membrane that described vacuum separates；And make to pass through described hydrophobicity from described heating seawater by the sea water in portion
Multiple aperture plasma membrane and be flowed in described vacuum steam cooling and condense cooling end；And decompressing unit, it makes described true
The decompression of empty portion, heating described sea water, described decompressing unit makes described for the heat of the thermal source using described ship for the described heater
The pressure of vacuum is that water passes through below the saturated vapour pressure under the ocean temperature in portion and 0.1atm in described heating seawater
Above pressure.
Described cooling end can possess：Cooling passes through portion with sea water, and it is for the sea water before described heating devices heat
Flow through；And cooling body, described cooling sea water is separated with described vacuum by it by portion.
The vacuum membrane distillation formula fresh water generator of above-mentioned ship can be to possess multiple described vacuum distilling modules, and
There is the sea water stream constituting as follows：Described sea water is in the cooling end by each vacuum distilling module with the order of regulation
Cooling with sea water behind portion by described heating devices heat, then passed through described each true with the order contrary with described order
The heating seawater of empty distillation module passes through portion.
Described decompressing unit can be made by conveying and powered water jet to described sea water.
The vacuum membrane distillation formula fresh water generator of above-mentioned ship can also be had and for described sea water to be transported to described water spray
The liquid transporting apparatus of device, described water jet is driven to the conveying of described sea water by described liquid transporting apparatus.
The vacuum membrane distillation formula fresh water generator of above-mentioned ship can also have：Fresh water container, it is with described vacuum even
Logical；And liquid carrying unit, the fresh water being condensed out in described vacuum is delivered to described fresh water container by it.
Described hydrophobic porous plasma membrane can comprise from by polysulfones, polyethylene, polypropylene, Kynoar and polytetrafluoro
At least one resin selecting in the group that ethylene is constituted.
The effect of invention
According to the present invention, in the vacuum membrane distillation formula fresh water generator of ship, can compactly realize height and make water efficiency.
Brief description
Fig. 1 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 1st embodiment
It is intended to.
Fig. 2 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 2nd embodiment
It is intended to.
Fig. 3 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 3rd embodiment
It is intended to.
Fig. 4 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 4th embodiment
It is intended to.
Fig. 5 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 5th embodiment
It is intended to.
Fig. 6 is the showing of the summary of structure of vacuum membrane distillation formula fresh water generator illustrating the ship in the 6th embodiment
It is intended to.
Fig. 7 is the curve chart illustrating the relation between the pressure of the vacuum in embodiment and amount of distilled water.
Specific embodiment
Below, referring to the drawings of the preferred embodiment of the present invention is illustrated.As long as and, especially not saying
Bright, the position relationship waiting up and down of accompanying drawing is based on position relationship shown in the drawings.The dimensional ratios of accompanying drawing are not limited to figure
The ratio shown.And, following embodiment is the illustration for the present invention is described, the present invention is not limited only to this embodiment.
In addition, the present invention just can carry out various modifications without departing from its purport.
(the 1st embodiment)
Fig. 1 is to illustrate the vacuum membrane distillation formula fresh water generator of ship of the present embodiment (in this manual only
Referred to as " fresh water generator ".) 1 the summary of structure explanatory diagram.The heat that vacuum membrane distillation formula fresh water generator 1 is had using ship
The heat in source, produces fresh water from the sea water being taken into ship.
Vacuum membrane distillation formula fresh water generator 1 for example possesses：The heater 10 of heating seawater；Carry out sea water distillation true
Empty distillation module 11；For carrying out the such as water jet 61 as decompressing unit of the conveying of sea water；And storage is generated
Fresh water container 13 of fresh water etc..
Vacuum distilling module 11 possesses：Pass through portion 20 for the heating seawater that sea water flows through；Vacuum 21；Heating seawater is led to
Cross the hydrophobic porous plasma membrane 22 that portion 20 and vacuum 21 separate；And the steam of vacuum 21 is cooled down and so that it is condensed
Cooling end 23.In vacuum distilling module 11, pass through the temperature difference between portion 20 and vacuum 21 and pressure by heating seawater
Power difference is so that flow into vacuum 21 by the steam that the sea water in portion 20 generates by hydrophobic porous plasma membrane 22 from heating seawater
In, the cooled portion 23 of this steam cools down and condenses.
Hydrophobic porous plasma membrane 22 employs for example resinous flat film.In addition, hydrophobic porous plasma membrane 22 employs and contains
There is the film of at least one resin selecting from following groups, wherein, this group is for example by polysulfones, polyethylene, polypropylene, poly- inclined fluorine
Ethylene and politef are constituted.
Cooling end 23 possesses：Pass through portion 30 for the cooling sea water that the sea water before being heated by heater 10 flows through；With
The coldplate 31 as cooling body that cooling sea water is separated with vacuum 21 by portion 30.
Between hydrophobic porous plasma membrane 22 and coldplate 31, it is formed between the distance for example less than the regulation of 10mm
Gap.
Vacuum membrane distillation formula fresh water generator 1 has：1st sea water stream 40, it will be extremely cold for the sea water supply being taken into ship
But passed through in portion 30 and decompressing unit such as water jet 61 with sea water；2nd sea water stream 41, it will pass through portion in cooling sea water
Sea water supply after passing through in 30 is to heater 10；3rd sea water stream 42, it will be supplied by the warmed-up sea water of heater 10
Pass through portion 20 to the heating seawater to vacuum distilling module 11；And the 4th sea water stream 43, it will pass through portion 20 in heating seawater
In by after sea water be discharged to the outside.
Heater 10 is, for example, heat exchanger, carries out heat exchange and can add between the heat of the thermal source of ship and sea water
Hot sea water.As the thermal source of ship, the used heat from Diesel engine or the steam from boiler etc. can be included.In addition,
With regard to heat exchange, heat exchange can be carried out via thermal medium and thermal source it is also possible to directly and thermal source carries out heat exchange.
Branch path 62 from the 1st sea water stream 40 branch is connected with water jet 61.Branch path 62 is provided with work
Ejector pump 63 for liquid transporting apparatus.Water jet 61 be made by by ejector pump 63 carry out from the 1st sea water stream 40 branch
The conveying of sea water and one kind of decompressing unit of driving, are connected with the upstream portion of water jet 61 and are connected with the top of vacuum 21
Vacuum draw road 60.In addition, the downstream of water jet 61 is connected with the 4th sea water stream 43.Passed through true using this water jet 61
Empty suction road 60 carries out vacuum draw to vacuum 21, vacuum 21 can be made to reduce pressure as water pass through the sea in portion 20 in heating seawater
Below saturated vapour pressure under coolant-temperature gage, 0.1atm (10.1325kPa).And, heating seawater is passed through to the sea water temperature in portion 20
Degree, such as inlet temperature, it is possible to use be arranged at thermocouple thermometer or the temperature detecting resistance temperature that heating seawater passes through portion 20
Count and to measure.In addition, water jet 61 can also use the fresh water obtained by sea water carries out Membrane Materials to be used as driving force.
Fresh water container 13 is reclaimed road 70 by fresh water and is communicated with the bottom of vacuum 21.Reclaim in fresh water and be provided with work on road 70
For the liquid delivery pump 71 of liquid carrying unit, the fresh water being condensed out in vacuum 21 is transported to light by this liquid delivery pump 71
Water container 13.Fresh water can be taken from fresh water container 13.
Next, saying to the water process of making in the vacuum membrane distillation formula fresh water generator 1 of the ship constituting above
Bright.First, the sea water being taken in ship is led to sea water by the cooling that the 1st sea water stream 40 is supplied to vacuum distilling module 11
Cross portion 30, and from cooling sea water, heater 10 is supplied to by the 2nd sea water stream 41 by portion 30.In this heater
In 10, sea water is heated to such as more than 50 DEG C by the heat of the thermal source from ship.Sea water after heating passes through the 3rd sea water stream 42
It is supplied to heating seawater and passes through portion 20, hereafter sea water is discharged by the 4th sea water stream 43.
Pass through in portion 20 in heating seawater, sea water becomes due to clipping the temperature difference of hydrophobic porous plasma membrane 22 and pressure differential
Become steam, and vacuum 21 is flowed into by hydrophobic porous plasma membrane 22.Now, vacuum 21 by water jet 61 be depressurized for
Water passes through the pressure of below the saturated vapour pressure under the ocean temperature in portion 20 and more than 0.1atm in heating seawater.Flow into vacuum
The cooled portion 23 of steam in 21 cools down and condenses.The fresh water so generating remains in the bottom of vacuum 21, and defeated by liquid
Send pump 71 to reclaim road 70 by fresh water to be recovered in fresh water container 13.
According to present embodiment, heater 10 by the hot heating seawater of the thermal source of ship, as the spray of decompressing unit
Hydrophone 61 vacuum 21 is reduced pressure as below saturated vapour pressure under heating seawater is by the ocean temperature in portion 20 for the water and
The pressure of more than 0.1atm.As a result, it is possible to the thermal efficiency improving fresh water generator 1 makes water efficiency additionally it is possible to be greatly improved.Cause
This, be capable of the fresh water generator of ship that is compact and making water efficiency high.
Because cooling end 23 possesses：Pass through portion for the cooling sea water that the sea water before being heated by heater 10 flows through
30；With the coldplate 31 that cooling sea water is separated with vacuum 21 by portion 30, it is therefore not necessary to cooling end 23 is supplied with new Jie
Matter, it is possible to increase the efficiency in fresh water generator.
Because the decompressing unit of vacuum 21 is made by the conveying of sea water and powered water jet 61, therefore need not newly set
Put driving source, it is possible to increase the efficiency in fresh water generator.
It is provided with liquid delivery pump 71 due to reclaiming in road 70 in fresh water, wherein, this liquid delivery pump 71 will be by vacuum
The fresh water of 21 condensations are transported in fresh water container 13, therefore, even if vacuum 21 by with higher vacuum decompression it is also possible to just
Local recovery fresh water.
(the 2nd embodiment)
In above-mentioned 1st embodiment, vacuum membrane distillation formula fresh water generator 1 can possess multiple, such as 2 vacuum distillinges
Module 11.In the present embodiment, 2 vacuum distilling modules are set to the 1st vacuum distilling module 11a and the 2nd vacuum distilling mould
Block 11b.
Vacuum membrane distillation formula fresh water generator 1 has the sea water stream for example constituting as follows：Sea water is according to the rules
The cooling end 23 by each vacuum distilling module 11a, 11b for the order cooling passed through behind portion 30 by heater 10 with sea water plus
Heat, then according to contrary order passes through portion 20 by the heating seawater of each vacuum distilling module 11a, 11b.
That is, sea water stream is made up of following part：1st sea water stream 100, it is by the sea water supply being taken in ship to
The cooling of 1 vacuum distilling module 11a passes through portion 30 with sea water；2nd sea water stream 101, it will be by the 1st vacuum distilling module
The cooling of 11a passes through portion 30 by the cooling of the sea water supply behind portion 30 to the 2nd vacuum distilling module 11b with sea water with sea water；
3rd sea water stream 102, it extremely adds passing through the sea water supply behind portion 30 with sea water by the cooling of the 2nd vacuum distilling module 11b
Thermal 10；4th sea water stream 103, it will be by the warmed-up sea water supply of heater 10 to the 2nd vacuum distilling module 11b
Heating seawater pass through portion 20；5th sea water stream 104, it will pass through portion by the heating seawater of the 2nd vacuum distilling module 11b
Sea water supply after 20 passes through portion 20 to the heating seawater of the 1st vacuum distilling module 11a；And the 6th sea water stream 105, it will
Pass through the sea water behind portion 20 to discharge by the heating seawater of the 1st vacuum distilling module 11a.
In addition, branch path 62 communicates from the 1st sea water stream 100 branch and with water jet 61.The downstream of water jet 61 with
5th sea water stream 105 communicates.Water jet 61 passes through the vacuum 21 on vacuum draw road 60 and each vacuum distilling module 11a, 11b
Connection.In addition, vacuum 21a of the fresh water recovery road 70 communicating with fresh water container 13 and each vacuum distilling module 11a, 11b,
21b connects.And, for the 1st embodiment identical part, using identical label and omit the description.
According to present embodiment, the cooling sea water of the 2nd vacuum distilling module 11b becomes to compare by the ocean temperature in portion 30
The ocean temperature that the cooling of the 1st vacuum distilling module 11a sea water passes through portion 30 is high, the heating sea of the 2nd vacuum distilling module 11b
The ocean temperature that water passes through portion 20 is higher than the ocean temperature that the heating seawater of the 1st vacuum distilling module 11a passes through portion 20.That is, exist
In each vacuum distilling module 11a, 11b, the ocean temperature that heating seawater passes through portion is different, can be set as and respective sea water temperature
Spend matched vacuum.Thus, in each vacuum distilling module 11a, 11b, can fully and rightly carry out the steaming of sea water
Evaporate and make water efficiency such that it is able to improve.And it is possible to make vacuum 21b of the 2nd vacuum distilling module 11b pressure ratio the 1st true
The pressure of vacuum 21a of empty distillation module 11a is high.
(the 3rd embodiment)
In above-mentioned 1st embodiment, flat film is employed but it is also possible to use doughnut to hydrophobic porous plasma membrane 22
Film.In this case, vacuum distilling module 110 for example can possess such as evaporation part 120 and condensation part as shown in Figure 3
121.Such as evaporation part 120 has the container of cylindrical shape, and possesses the length direction (upper and lower in container in the inside of this container
To) hollow-fibre membrane 123 of the pencil as hydrophobic porous plasma membrane of upper configuration.Primary side (the pipe of this hollow-fibre membrane 123
Inner side) connect with the 3rd sea water stream 42 and the 4th sea water stream 43.Condensation part 121 has for example is justified with evaporation part 120 identical
The container of tubular, and possess the cooling tube 124 as cooling body of configuration on the length direction of container inside this container.Cold
But connect with the 1st sea water stream 40 and the 2nd sea water stream 41 in the pipeline of pipe 124.Evaporation part 120 and condensation part 121 are abreast
It is arranged side-by-side, and interconnected by the connection space 125 configuring between them.Vacuum draw road 60 and connection space 125
Connect.Therefore, in the present embodiment, the space of the primary side (inside pipe) in hollow-fibre membrane 123 for the evaporation part 120 becomes and adds
Hot sea water passes through portion 20, outside the space of secondary side (outside) of hollow-fibre membrane 123, connection space 125 and cooling tube 124
Side space becomes vacuum 21, becomes cooling sea water and pass through portion 30 in the pipeline of cooling tube 124.Fresh water reclaim road 70 for example with
The outer space of the following cooling tube 124 of condensation part 121 connects.And, for the 1st embodiment identical part, make
With identical label and omit the description.
In this case, sea water is passed through portion 30 by the cooling supplying to cooling tube 124 from the 1st sea water stream 40 with sea water
In, and from cooling tube 124, heater 10 is supplied to by the 2nd sea water stream 41.By the warmed-up sea water of heater 10
Portion 20 is passed through by the heating seawater that the 3rd sea water stream 42 is supplied to the primary side in hollow-fibre membrane 123 for the evaporation part 120
In.It is supplied to heating seawater by the sea water in portion 20 due to clipping the primary side of hollow-fibre membrane 123 and the temperature of secondary side
Spend difference and pressure differential and become steam, and true by the secondary side of the side wall inflow hollow-fibre membrane 123 of hollow-fibre membrane 123
In empty portion 21.Now, vacuum 21 is depressurized by water jet 61 and passes through under the ocean temperature in portion 20 in heating seawater for water
Below saturated vapour pressure and more than 0.1atm pressure.Flow into the steam in the vacuum 21 of secondary side of hollow-fibre membrane 123
Reach the cooling tube 124 of condensation part 121 through connection space 125, be cooled herein and condense.The fresh water so generating retains
In the bottom of condensation part 121, and it is recovered in fresh water container 13 by fresh water recovery road 70 by liquid delivery pump 71.
According to present embodiment, can the save space and membrane area of hydrophobic porous plasma membrane 22 can be increased, therefore, film
The amount of distilled water (Flux) of per unit area increase, it is possible to increase making water efficiency and make the water yield in fresh water generator 1.Therefore,
Height can compactly be realized in the fresh water generator 1 of ship and make water efficiency.
(the 4th embodiment)
Can also be replaced using hollow-fibre membrane 123 for hydrophobic porous plasma membrane 22 in above-mentioned 2nd embodiment
Flat film.Using vacuum distilling module 110a, 110b of hollow-fibre membrane 123 can have as shown in Figure 4 with the above-mentioned 3rd
Vacuum distilling module 110 identical structure used in embodiment.
In this case, sea water is supplied to the condensation part 121 of the 1st vacuum distilling module 110a from the 1st sea water stream 100
Cooling tube 124 in, and supplied to the 2nd true from the cooling tube 124 of the 1st vacuum distilling module 110a by the 2nd sea water stream 101
In the cooling tube 124 of empty distillation module 110b, then pass through the 3rd sea water stream from the cooling tube 124 of the 2nd vacuum distilling module 110b
102 supply to heater 10.2nd vacuum is supplied to by the 4th sea water stream 103 by the warmed-up sea water of heater 10
The primary side (heating seawater passes through portion 20) of the hollow-fibre membrane 123 of evaporation part 120 of distillation module 110b, then passes through the 5th
Sea water stream 104 be supplied to the hollow-fibre membrane 123 of the 1st vacuum distilling module 110b primary side (heating seawater pass through portion
20).This rear sea water is discharged by the 6th sea water stream 105.According to present embodiment, can be further with small-sized fresh water generator 1
Improve and make the water yield and make water efficiency.
(the 5th embodiment)
In the above embodiment, from the respective vacuum of 2 vacuum distilling modules carry out respectively fresh water discharge and
Aerofluxuss but it is also possible to as shown in Figure 5, the fresh water of vacuum 21b of the 2nd vacuum distilling module 11b are reclaimed road 70 and true
Empty suction road 60 is connected with vacuum 21a of the 1st vacuum distilling module 11a, by the vacuum in the 2nd vacuum distilling module 11b
The fresh water generating in 21b supplies vacuum 21a to the 1st vacuum distilling module 11a and the mixing of fresh water with vacuum 21a, and
This fresh water is discharged to returnable 13 from vacuum 21a.Alternatively, it is also possible to by the vacuum of the 2nd vacuum distilling module 11b
The gas of 21b is pumped to vacuum 21a, and is pumped to water jet 61 from this vacuum 21a.In this case, for example can be
In vacuum 21a utilize vacuum 21b heat, therefore, it is possible to reduce heater 10 with heat such that it is able to improve make water
The thermal efficiency of device.And, this is also applied for the situation of the use film module as shown in the 4th embodiment.
(the 6th embodiment)
In the above embodiment, the water jet 61 as decompressing unit is driven by the conveying of sea water, but
Can be driven by the conveying to the fresh water producing from sea water.In this case, for example as shown in fig. 6, fresh water reclaims
Road 70 is connected with returnable 13 via water jet 61.In addition, circulation road 130, this circulation road are connected with returnable 13
130 make the fresh water (manufacture water) of returnable 13 return water jet 61 is circulated.Circulation road 130 is provided with pump 131.This
In the case of, for example the fresh water in returnable 13 is delivered to by water jet 61 by the driving of pump 131, thus, water jet 61 moves
Make, so that vacuum 21 is reduced pressure by vacuum draw road 60.In addition, now the fresh water of vacuum 21 can be reclaimed road by fresh water
70 and be discharged to returnable 13 via water jet 61.And, this example can be applied to above-mentioned all of embodiment.
Although above referring to the drawings and being preferred embodiment illustrated to the present invention, the invention is not restricted to institute
The example being related to.It should be appreciated that it is evident that being capable of thought category described in claims for those skilled in the art
Inside expect various modifications or modification, these modifications or modification also would naturally fall within the technical scope of the present invention.
For example in the above embodiment, as vacuum distilling module 11,11a, 11b, 110, the cooling of 110a, 110b
The cold-producing medium in portion 23, employs the sea water before heating but it is also possible to use other cold-producing mediums.In addition, as decompressing unit,
Employ water jet 61 but it is also possible to use other decompressing unit such as pump, getter.The structure of decompressor is also not necessarily limited to above-mentioned
The water jet of embodiment.
Embodiment
Hereinafter, illustrate for specifically illustrating the structure of the present invention and the embodiment of effect etc., but present embodiment is complete
Entirely it is not limited to below example.
(embodiment 1)
Be used thickness to be 190 μm, molecular cut off be 500kDa the flat film of polysulfones system (Sepro society system) many as hydrophobicity
Hole plasma membrane 22, is used the corrosion resistant plate for 2mm for the thickness as coldplate 31, and is adjusted using distance piece, so that shown in Fig. 1
Hydrophobic porous plasma membrane 22 become 4mm with the distance between coldplate 31 (Gap).Make 30 DEG C with the flow of 600mL/min
Simulated seawater (3.5 weight % sodium-chloride water solution) flows, and heating seawater is adjusted to 65 DEG C by the inlet temperature in portion 20.Make
With vacuum pump or vacuum control unit, the pressure adjustment in vacuum 21 is become 0.10atm, carry out Membrane Materials.Start in experiment
Take out, after 30 minutes, the water remaining in fresh water container 13, and calculate Flux, obtained 25.0kg/m2High level (the 10.0kg/ of/h
m2The value of/more than h).In addition, the conductivity of the membrane distillation water obtaining is 0.0 μ S/cm when 25 DEG C.And, water sea at this moment
Saturated water vapor pressure under coolant-temperature gage (65 DEG C) is of about 0.25atm.
(embodiment 2)
Except by the Gap (distance) between hydrophobic porous plasma membrane 22 and coldplate 31 be changed to 10mm with replace 4mm it
Outward, Membrane Materials have been carried out using method same as Example 1.Take out after experiment starts 30 minutes and remain in water intaking container
Water, as shown in fig. 7, obtained Flux be 24.1kg/m2The value of/h.In addition, the conductivity of the membrane distillation water obtaining is at 25 DEG C
When be 0.0 μ S/cm.
(embodiment 3)
Except the pressure of vacuum 21 is changed to 0.20atm to replace 0.10atm in addition to, using same as Example 2
Method carried out Membrane Materials.As shown in fig. 7, having obtained Flux is 11.1kg/m2The value of/h.In addition, the membrane distillation water obtaining
Conductivity when 25 DEG C be 0.1 μ S/cm.
(embodiment 4)
Employ the hydrophobic porous plasma membrane 22 of the flat film of the polysulfones system using in embodiment 1 and the coldplate of corrosion resistant plate
31, and be adjusted using distance piece, so that hydrophobic porous plasma membrane 22 becomes 2mm with the distance between coldplate 31 (Gap).
Link 2 groups of vacuum distilling modules 11a, 11b as shown in Figure 2, make 30 DEG C of simulated seawater (3.5 weight % aqueous sodium chloride
Liquid) with the traffic flow of 600mL/min, it is adjusted, so that the inlet temperature of the evaporation part 120 of vacuum distilling module 11a becomes
For 65 DEG C, make the inlet temperature of condensation part 121 become 50 DEG C, so that the inlet temperature of the evaporation part 120 of vacuum distilling module 11b is become
For 47 DEG C, and the inlet temperature of condensation part 121 is made to become 30 DEG C.1st vacuum distilling module 11a and the 2nd vacuum distilling module 11b
The pressure of respective vacuum 21a, 21b is adjusted separately, and so that becomes in vacuum 21a of the 1st vacuum distilling module 11a
The mode that pressure for 0.24atm, in vacuum 21b that makes the 2nd vacuum distilling module 11b becomes 0.10atm is adjusted, and
Membrane Materials are carried out.Take out, after experiment starts 30 minutes, the water remaining in fresh water container 13, and calculate Flux, obtain
11.2kg/m2The value of/h.In addition, the conductivity of the membrane distillation water obtaining is 0.1 μ S/cm when 25 DEG C.
(comparative example 1)
Saturation except being set to pass through under the ocean temperature in portion 20 in heating seawater the pressure of vacuum 21 than water is steamed
Outside the high atmospheric pressure of air pressure, Membrane Materials are carried out using method same as Example 1.Take out after experiment starts 30 minutes
Remain in the water in fresh water container 13, and calculate Flux, obtain 3.3kg/m2The value of/h.In addition, the membrane distillation water obtaining
Conductivity is 0.1 μ S/cm when 25 DEG C.
(comparative example 2)
Except the pressure of vacuum 21 is changed to 0.30atm to replace 0.10atm in addition to, using same as Example 2
Method carried out Membrane Materials.As shown in fig. 7, having obtained Flux is 5.5kg/m2The value of/h.In addition, the membrane distillation water obtaining
Conductivity is 0.2 μ S/cm when 25 DEG C.
(comparative example 3)
Except the pressure of vacuum 21 is changed to 0.50atm to replace 0.10atm in addition to, using same as Example 2
Method carried out Membrane Materials.As shown in fig. 7, having obtained Flux is 3.0kg/m2The value of/h.In addition, the membrane distillation water obtaining
Conductivity is 0.2 μ S/cm when 25 DEG C.
(comparative example 4)
In addition to the pressure of vacuum 21a, 21b in 2 groups of vacuum distilling modules 11a, 11b is arranged to atmospheric pressure,
Membrane Materials are carried out using method same as Example 2.Take out after experiment starts 30 minutes and remain in fresh water container 13
Water, and calculate Flux, obtained 3.4kg/m2The value of/h.In addition, the conductivity of the membrane distillation water obtaining is 0.3 when 25 DEG C
μS/cm.
Industrial applicability
The present invention is when providing the vacuum membrane distillation formula fresh water generator that can compactly realize the ship that height makes water efficiency
Useful.
Label declaration
1：The membrane distillation type fresh water generator of ship；
10：Heater；
11：Vacuum distilling module；
13：Fresh water container；
20：Heating seawater passes through portion；
21：Vacuum；
22：Hydrophobic porous plasma membrane；
23：Cooling end；
61：Water jet.
Claims (7)
1. the vacuum membrane distillation formula fresh water generator of a kind of ship, the heat of its thermal source being had using ship is from being taken into ship
Sea water in produce fresh water, wherein,
The vacuum membrane distillation formula fresh water generator of this ship has：
Heater, it heats to the sea water being taken into ship；
Vacuum distilling module, it possesses：Pass through portion for the heating seawater that the sea water after described heating devices heat flows through；Vacuum
Portion；The hydrophobic porous plasma membrane that described heating seawater is separated by portion and described vacuum；And make from described heating seawater
The cooling that the steam being flowed into by described hydrophobic porous plasma membrane by the sea water in portion in described vacuum is cooled down and condenses
Portion；And
Decompressing unit, it makes described vacuum decompression,
The heat of the thermal source using described ship for the described heater heating described sea water,
Described decompressing unit makes the saturation steaming that described vacuum reduces pressure as water under the ocean temperature by portion for the described heating seawater
Below air pressure and more than 0.1atm pressure.
2. the vacuum membrane distillation formula fresh water generator of ship according to claim 1, wherein,
Described cooling end possesses：
Cooling passes through portion with sea water, and it is for being flow through by the sea water before described heating devices heat；With
Cooling body, described cooling sea water is separated with described vacuum by it by portion.
3. the vacuum membrane distillation formula fresh water generator of ship according to claim 2, wherein,
The vacuum membrane distillation formula fresh water generator of described ship possesses multiple described vacuum distilling modules,
And there is the sea water stream constituting as follows：Described sea water with regulation order by each vacuum distilling module
Cooling end cooling with sea water behind portion by described heating devices heat, then passed through with the order contrary with described order
The heating seawater of described each vacuum distilling module passes through portion.
4. the vacuum membrane distillation formula fresh water generator of the ship according to any one in claims 1 to 3, wherein,
Described decompressing unit is made by the conveying to described sea water or the conveying to the fresh water producing from described sea water and is driven
Dynamic water jet.
5. the vacuum membrane distillation formula fresh water generator of ship according to claim 4, wherein,
The vacuum membrane distillation formula fresh water generator of described ship also have by described sea water be transported to described water jet liquid defeated
Send device,
Described water jet is driven to the conveying of described sea water by described liquid transporting apparatus.
6. the vacuum membrane distillation formula fresh water generator of the ship according to any one in Claims 1 to 5, wherein,
The vacuum membrane distillation formula fresh water generator of described ship also has：
Fresh water container, it is connected with described vacuum；With
Liquid carrying unit, the fresh water being condensed out in described vacuum is delivered to described fresh water container by it.
7. the vacuum membrane distillation formula fresh water generator of the ship according to any one in claim 1～6, wherein,
Described hydrophobic porous plasma membrane comprises from being made up of polysulfones, polyethylene, polypropylene, Kynoar and politef
Group in select at least one resin.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2014-142548 | 2014-07-10 | ||
| JP2014142548 | 2014-07-10 | ||
| PCT/JP2015/069803 WO2016006666A1 (en) | 2014-07-10 | 2015-07-09 | Vacuum membrane distillation desalination device for ship |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106470753A true CN106470753A (en) | 2017-03-01 |
| CN106470753B CN106470753B (en) | 2020-08-28 |
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| CN201580035241.2A Active CN106470753B (en) | 2014-07-10 | 2015-07-09 | Vacuum membrane distillation type water making device for ship |
Country Status (5)
| Country | Link |
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| JP (1) | JP6303009B2 (en) |
| KR (1) | KR101852709B1 (en) |
| CN (1) | CN106470753B (en) |
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| WO (1) | WO2016006666A1 (en) |
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| CN110130470A (en) * | 2019-05-29 | 2019-08-16 | 上海新三星给排水设备有限公司 | A kind of prefabricated pumping plant of hands-free basket and sewage disposal system |
| CN110342600A (en) * | 2019-07-04 | 2019-10-18 | 浙江大学 | A kind of membrane distillation purified water preparation system of injector driving |
| CN111039354A (en) * | 2018-10-12 | 2020-04-21 | 卫风科技股份有限公司 | Filter system and operation method thereof |
| CN113479971A (en) * | 2021-07-13 | 2021-10-08 | 中国核动力研究设计院 | System for desalinate sea water in lead bismuth alloy coolant device |
| CN113578005A (en) * | 2021-08-17 | 2021-11-02 | 承德建龙特殊钢有限公司 | Flue gas circulating fluidized bed semidry method desulfurization method |
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| KR102027538B1 (en) * | 2018-01-18 | 2019-10-01 | 삼성중공업 주식회사 | Fresh water generator device |
| JP7250325B2 (en) | 2019-05-28 | 2023-04-03 | 株式会社ササクラ | Membrane distillation system |
| CN110479102A (en) * | 2019-09-03 | 2019-11-22 | 盐城海普润膜科技有限公司 | Pervaporation desalination anisotropic membrane and preparation method thereof |
| KR102257887B1 (en) * | 2019-09-20 | 2021-05-28 | 주식회사 알이디 | THE MEMBRANE DISTILLATION APPARATUS in which the DEAD-ZONE is controlled |
| US11413581B2 (en) | 2020-02-24 | 2022-08-16 | King Fahd University Of Petroleum And Minerals | Bubble feed membrane distillation system |
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Also Published As
| Publication number | Publication date |
|---|---|
| KR101852709B1 (en) | 2018-04-26 |
| JPWO2016006666A1 (en) | 2017-04-27 |
| WO2016006666A1 (en) | 2016-01-14 |
| TW201605739A (en) | 2016-02-16 |
| CN106470753B (en) | 2020-08-28 |
| TWI561474B (en) | 2016-12-11 |
| JP6303009B2 (en) | 2018-03-28 |
| KR20170002698A (en) | 2017-01-06 |
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