CN208066148U - A kind of vacuum type multiple-effect membrane distillation system - Google Patents
A kind of vacuum type multiple-effect membrane distillation system Download PDFInfo
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- CN208066148U CN208066148U CN201820318307.XU CN201820318307U CN208066148U CN 208066148 U CN208066148 U CN 208066148U CN 201820318307 U CN201820318307 U CN 201820318307U CN 208066148 U CN208066148 U CN 208066148U
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Abstract
The utility model is related to film distillation technology fields, disclose a kind of vacuum type multiple-effect membrane distillation system, including：Vapour compression machine, the second heat exchanger, third heat exchanger, the second membrane distiller and multiple membrane components；Membrane component includes First Heat Exchanger and the first membrane distiller, its by membrane distiller with vapour compression machine be combined in the way of material liquid is concentrated, be used for preheating material liquid after its both vapor compression for the first membrane distiller being generated in the way of multi-stage heat exchanger, and heating heating is carried out to next effect material liquid by the sensible heat of effect steam before recycling and latent heat, the energy consumption for supplementing feed liquid evaporation.The problems such as the utility model overcomes traditional membrane distillation process heat utilization efficiency low, and distillation process is complicated, and energy consumption is larger, has fully considered the cascade utilization of the energy, has greatly reduced the energy consumption of distillation process, played the effect of energy-saving and emission-reduction well.
Description
Technical field
The utility model is related to film distillation technology fields, more particularly to a kind of vacuum type multiple-effect membrane distillation system.
Background technology
The research of membrane distillation (membrane distillation, MD) technology started from application in the 1960s, until
At the beginning of the eighties, with the rapid development of high molecular material and film preparation technology, membrane distillation just shows its practical potentiality.Root
The difference of side condensing mode is penetrated according to film, membrane distillation can be divided into direct contact membrane distillation (DCMD), vacuum membrane distillation
(VMD), 4 kinds of forms of gap field orientation (AGMD) and sweep gas membrane disillation (SGMD).It is gradually light from seawater and bitter
The water purifications research such as change, expands to the concentration of chemical substance and heat-sensitive substance and the removing of volatile solutes in recycling, aqueous solution
With the numerous areas such as recycling, wastewater treatment, at present at the beginning of the concentration of tea extract, soybean protein isolate, concentration of juices, ox
Breast, the preparation of amino acid, the concentration of part material liquid etc. have certain application, further include the mass transfer of different systems, pass
Research in terms of the mechanism such as heat.
Membrane distillation is a kind of to use dewatering microporous film using film both sides vapor pressure differential as the membrane separating process of mass transfer driving force.
During membrane distillation, evaporable water will necessarily consume a large amount of industrial steam or electric energy, and the moisture for often evaporating 1kg just needs to disappear
Consume the heating steam more than 1kg or the electric energy more than 0.628kWh.Its mechanism is the aqueous solution when different temperatures by hydrophobic microporous
When film separates, due to the hydrophobicity of film, the aqueous solution of both sides cannot enter the other side through fenestra, but since hot side is water-soluble
The water vapor pressure of liquid and membrane interface is higher than cold side, and water vapour will enter cold side from hot side through fenestra and condense to realize dense
Contracting.The process and the evaporation in conventional distil-lation, mass transfer, condensation process are quite similar, so being called membrane distillation process.It has
Four main features：First, film is dewatering microporous film, cannot be soaked by handled liquid, only steam can pass through fenestra；Two
It is that film at least one side is contacted with handled liquid, does not have capillary condensation phenomenon in fenestra；Third, film cannot change
The vapor liquid equilibrium of all components in handled liquid；Fourth, the motive force of membrane process is the partial pressure difference of the component in the gas phase.
But current membrane distillation technique heat utilization efficiency is low, and complex procedures, energy consumption is larger, do not meet current energy-saving and emission-reduction when
For background.
Utility model content
(1) technical problems to be solved
The purpose of this utility model is to provide a kind of vacuum type multiple-effect membrane distillation system, solves vacuum type film in the prior art
Distillation technique system process complexity and the larger problem of energy consumption.
(2) technical solution
In order to solve the above-mentioned technical problem, the utility model provides a kind of vacuum type multiple-effect membrane distillation system, including：Steam
Compressor, the second heat exchanger, third heat exchanger, the second membrane distiller and multiple membrane components；
Each membrane component includes First Heat Exchanger and the first membrane distiller, and the First Heat Exchanger includes first
Import, first outlet, the second import and second outlet, first membrane distiller include third import, third outlet and the 4th
Outlet, second import connection of the corresponding First Heat Exchanger in the 4th outlet of first membrane distiller,
First import of the First Heat Exchanger and the third outlet of the first membrane distiller described in its latter connect, described
The first outlet of First Heat Exchanger is connect with the third import of the first membrane distiller described in its latter, and described first
The second outlet of heat exchanger is connect with second import of First Heat Exchanger described in its latter；
Second heat exchanger include the 5th import, the 5th outlet, the 6th import and the 6th outlet, the 5th import with
Material liquid import connects, and the 6th outlet is connect with condensate outlet；
The third heat exchanger include the 7th import, the 7th outlet, the 8th import and the 8th outlet, the 7th import with
5th outlet connection, the 8th outlet connects with the 6th import, the 7th outlet and are in the described in head end
The third import of one membrane distiller connects；
Second membrane distiller include the 9th import, the 9th outlet and the tenth outlet, the 9th import in end
The first outlet of the First Heat Exchanger is held to connect, the described 9th exports and be in the described of First Heat Exchanger described in end
First import connects；
Tenth outlet passes through the both vapor compression with the second outlet in First Heat Exchanger described in end
Machine is connect with the 8th import.
Wherein, the membrane component further includes the first gas-liquid separator, the gas-liquid separator include the 11st import,
11st outlet and the 12nd outlet, the corresponding First Heat Exchanger of the 11st import of the gas-liquid separator
The second outlet connection, the 11st outlet connect with second import of First Heat Exchanger described in its latter, locate
11 outlet of the gas-liquid separator described in end is connect by the vapour compression machine with the 8th import, and described the
12 outlets are connect with the condensate outlet.
Wherein, the membrane component further includes the second solution pump, and second solution pump is set to first entrance.
Wherein, the membrane component further includes the second material liquid tank, second material liquid tank one end and second solution
Pump connection, the third outlet connection of corresponding first membrane distiller of the other end.
Wherein, further include the second gas-liquid separator, the gas-liquid separator includes the tenth triple feed inlet, the 13rd outlet and the
14 outlets, the tenth triple feed inlet go out with 11 outlet and the described tenth in gas-liquid separator described in end respectively
Mouth connection, the 14th outlet are connect with the condensate outlet.
Wherein, further include the first solution pump, first solution pump is set to the 7th exit.
Wherein, further include the first material liquid tank, first material liquid tank includes the 15th import, the 15th outlet and the 16th
Import, the 15th import are connected with the third outlet in the first membrane distiller described in head end, and the described 15th goes out
Mouth is connect with the 7th import, and the 16th import is connected with the 5th outlet.
Wherein, first material liquid tank and second material liquid tank are equipped with heating device.
Wherein, the vapour compression machine is centrifugal compressor or helical-lobe compressor.
Wherein, the membrane component is two.
(3) advantageous effect
A kind of vacuum type multiple-effect membrane distillation system provided by the utility model utilizes membrane distiller and vapour compression machine phase
In conjunction with mode material liquid is concentrated, in the way of multi-stage heat exchanger by compressed steam be used for preheating material liquid,
And heating heating is carried out to next effect material liquid by the sensible heat of effect steam before recycling and latent heat, for supplementing feed liquid evaporation
Energy consumption, this mode can make distillation process flexible, continue, and stablize and carry out, and can carry out different material liquid flexible
Collocation.The problems such as the utility model overcomes traditional membrane distillation process heat utilization efficiency low, and distillation process is complicated, and energy consumption is larger, fills
Divide the cascade utilization for considering the energy, greatly reduces the energy consumption of distillation process, play the effect of energy-saving and emission-reduction well
Fruit.
Description of the drawings
Fig. 1 is a kind of structural schematic diagram of vacuum type multiple-effect membrane distillation system of the utility model.
In figure, 1, vapour compression machine；2, the second heat exchanger；3, third heat exchanger；4, First Heat Exchanger；5, the first membrane distillation
Device；6, the second membrane distiller；7, the first gas-liquid separator；8, the second solution pump；9, the second material liquid tank；10, the second gas-liquid separation
Device；11, the first solution pump；12, the first material liquid tank；13, condensate drum.
Specific implementation mode
With reference to the accompanying drawings and examples, specific embodiment of the present utility model is described in further detail.Below
Example is not intended to limit the scope of the present invention for illustrating the utility model.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " is pacified
Dress ", " connected ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integrally
Connection；It can be mechanical connection, can also be electrical connection；Can be directly connected, can also indirectly connected through an intermediary,
It can be the connection inside two elements.For the ordinary skill in the art, it can understand above-mentioned art with concrete condition
The concrete meaning of language in the present invention.
As shown in Figure 1, the utility model discloses a kind of vacuum type multiple-effect membrane distillation system, including：Vapour compression machine 1,
Two heat exchangers 2, third heat exchanger 3, the second membrane distiller 6 and multiple membrane components；
Each membrane component includes First Heat Exchanger 4 and the first membrane distiller 5, and the First Heat Exchanger 4 includes
First import, first outlet, the second import and second outlet, first membrane distiller 5 include third import, third outlet and
4th outlet, the described 4th of first membrane distiller 5 the exports second import of the corresponding First Heat Exchanger 4
Connection, first import of the First Heat Exchanger 4 connect with the third outlet of the first membrane distiller 5 described in its latter
It connects, the first outlet of the First Heat Exchanger 4 connects with the third import of the first membrane distiller 5 described in its latter
It connects, the second outlet of the First Heat Exchanger 4 is connect with second import of First Heat Exchanger 4 described in its latter；
Second heat exchanger 2 includes the 5th import, the 5th outlet, the 6th import and the 6th outlet, the 5th import
It is connect with material liquid import, the 6th outlet is connect with condensate outlet；
The third heat exchanger 3 includes the 7th import, the 7th outlet, the 8th import and the 8th outlet, the 7th import
It is connected with the 5th outlet, the 8th outlet is connect with the 6th import, and the described 7th exports and in described in head end
The third import of first membrane distiller 5 connects；
Second membrane distiller 6 include the 9th import, the 9th outlet and the tenth outlet, the 9th import in end
The first outlet of the First Heat Exchanger 4 is held to connect, the 9th outlet and the institute in First Heat Exchanger 4 described in end
State the first import connection；
Tenth outlet passes through the both vapor compression with the second outlet in First Heat Exchanger 4 described in end
Machine 1 is connect with the 8th import.
It is worth noting that, " correspondence " refers to the corresponding intrument in the same membrane component, " being in head end " refers to
Close to material liquid entrance, " being in end " refers to close to condensate outlet.
Specifically, the 5th import and the 5th outlet become the 5th heat exchanging pipe, the 6th import and the 6th outlet
As the 6th heat exchanging pipe, the 5th heat exchanging pipe and the 6th heat exchanging pipe exchange heat, using high temperature biphase gas and liquid flow to material liquid into
The first preheating of row.7th import and the 7th outlet become the 7th heat exchanging pipe, and the 8th import and the 8th outlet become
8th heat exchanging pipe, the 7th heat exchanging pipe and the heat exchange of the 8th heat exchanging pipe carry out material liquid using high temperature and high pressure steam secondary
Preheating.First import is connected to first outlet becomes the first heat exchanging pipe, and the second import is connected to second outlet changes as second
Pipe line, the first heat exchanging pipe and the heat exchange of the second heat exchanging pipe, using the sensible heat and latent heat of preceding effect steam come to next effect raw material
Liquid carries out heating heating, the energy consumption for supplementing feed liquid evaporation.5 and second membrane distiller 6 of multiple first membrane distillers can be realized
Multistage concentration, the steam that the first membrane distiller 5 generates are passed through the second heat exchanging pipe, exchange heat with material liquids at different levels
Low temperature and low pressure steam can be compressed into high temperature and high pressure steam by vapour compression machine 1, be used for heating up for material liquid, may be used also
Vacuum environment is provided with the steam side for membrane distiller, adjusts inlet side quantity of steam.Utilize vapour compression machine 1, the second heat exchanger 2
It is preheated for the first time with third heat exchanger 3 and secondary preheating.It is internal comprising distillation film for membrane distiller, is that a kind of use is hydrophobic micro-
Pore membrane is using film both sides vapor pressure differential as the membrane separating process of mass transfer driving force.Its mechanism is when the aqueous solution of different temperatures is dredged
When water microporous barrier separates, due to the hydrophobicity of film, the aqueous solution of both sides cannot enter the other side through fenestra, but due to heat
The water vapor pressure of side aqueous solution and membrane interface be higher than cold side, water vapour will through fenestra from hot side enter cold side and condense to
Realize concentration.The steam that First Heat Exchanger 4 in multiple membrane components is discharged using membrane distiller carries out material liquid multistage
Heating.The membrane component of different number can be selected according to different actual needs and technological requirement.
A kind of vacuum type multiple-effect membrane distillation system provided by the utility model utilizes membrane distiller and vapour compression machine phase
In conjunction with mode material liquid is concentrated, in the way of multi-stage heat exchanger by compressed steam be used for preheating material liquid,
And heating heating is carried out to next effect material liquid by the sensible heat of effect steam before recycling and latent heat, for supplementing feed liquid evaporation
Energy consumption, this mode can make distillation process flexible, continue, and stablize and carry out, and can carry out different material liquid flexible
Collocation.The problems such as the utility model overcomes traditional membrane distillation process heat utilization efficiency low, and distillation process is complicated, and energy consumption is larger, fills
Divide the cascade utilization for considering the energy, greatly reduces the energy consumption of distillation process, play the effect of energy-saving and emission-reduction well
Fruit.
Wherein, the membrane component further includes the first gas-liquid separator 7, the gas-liquid separator include the 11st into
Mouth, the 11st outlet and the 12nd outlet, corresponding first heat exchange of the 11st import of the gas-liquid separator
The second outlet of device 4 connects, and the 11st outlet and second import of First Heat Exchanger 4 described in its latter connect
It connecing, 11 outlet in gas-liquid separator described in end is connect by the vapour compression machine 1 with the 8th import,
12nd outlet is connect with the condensate outlet.The present embodiment second outlet discharge steam and or condensed water be not
It is directly connect with vapour compression machine 1, but utilizes the first gas-liquid separator 7 by after condensed water and steam separation, steam passes through steaming
Vapour compressor 1 is collapsed into the steam of high temperature and pressure, is exchanged heat to material liquid by the second heat exchanger 2 and third heat exchanger 3, and cold
Condensate is then expelled directly out.
Preferably, the membrane component further includes the second solution pump 8, second solution pump 8 be set to described first into
At mouthful, for providing circulation power to the material liquid in membrane component.
Preferably, the membrane component further includes the second material liquid tank 9, described second material liquid tank, 9 one end and described second
Solution pump 8 connects, the third outlet connection of corresponding first membrane distiller of the other end 5.Material in second material liquid tank 9
Liquid concentration constantly rises with the propulsion of process.After concentration reaches requirement, feed liquid is separately replaced, has the function of adjusting concentration.
Wherein, further include the second gas-liquid separator 10, the gas-liquid separator include the tenth triple feed inlet, the 13rd outlet and
14th outlet, the tenth triple feed inlet respectively in gas-liquid separator described in end it is described 11 outlet and the described tenth
Outlet connection, the 14th outlet are connect with the condensate outlet.The steam of the present embodiment is not straight with vapour compression machine 1
It connects in succession, the second gas-liquid separator 10 receives the steam and/condensed water of the second membrane distiller 6, and detaches condensed water from condensed water
Outlet discharge, steam are then passed through after vapour compression machine 1 is compressed into the steam of high pressure-temperature and supply the second heat exchanger 2 and third heat exchanger
3 heat exchange use.
Preferably, condensate drum 13, recycling and storage condensate liquid are set at condensate outlet.
Further include the first solution pump 11, first solution pump 11 is set to the 7th exit, will enter for giving
The material liquid of first membrane distiller 5 provides circulation power.
Further include the first material liquid tank 12, first material liquid tank 12 includes the 15th import, the 15th outlet and the 16th
Import, the 15th import are connected with the third outlet in the first membrane distiller 5 described in head end, and the described 15th goes out
Mouth is connect with the 7th import, and the 16th import is connected with the 5th outlet.Its main function is that material liquid is dense
Contracting liquid returns liquid and is mixed with material liquid, to be that Aqueous extracts are concentrated to certain concentration and provide mixing volume.The present embodiment second changes
The material liquid of hot device 2 is not directly connected to third heat exchanger 3, is concentrated to material liquid using solution tempering tank specific dense
The heat exchange of third heat exchanger 3 is passed through after degree again.
Preferably, first material liquid tank 12 and second material liquid tank 9 are equipped with heating device, carry out lifting system unlatching
When material liquid temperature.
Wherein, the vapour compression machine 1 is centrifugal compressor or helical-lobe compressor.
As shown in Figure 1, the present embodiment membrane component is two.
A kind of vacuum type multiple-effect membrane distillation system provided by the utility model utilizes membrane distiller and vapour compression machine phase
In conjunction with mode material liquid is concentrated, in the way of multi-stage heat exchanger by compressed steam be used for preheating material liquid,
And heating heating is carried out to next effect material liquid by the sensible heat of effect steam before recycling and latent heat, for supplementing feed liquid evaporation
Energy consumption, this mode can make distillation process flexible, continue, and stablize and carry out, and can carry out different material liquid flexible
Collocation.The problems such as the utility model overcomes traditional membrane distillation process heat utilization efficiency low, and distillation process is complicated, and energy consumption is larger, fills
Divide the cascade utilization for considering the energy, greatly reduces the energy consumption of distillation process, play the effect of energy-saving and emission-reduction well
Fruit.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on should be included in the utility model
Protection domain within.
Claims (10)
1. a kind of vacuum type multiple-effect membrane distillation system, which is characterized in that including：Vapour compression machine (1), the second heat exchanger (2),
Three heat exchangers (3), the second membrane distiller (6) and multiple membrane components；
Each membrane component includes First Heat Exchanger (4) and the first membrane distiller (5), First Heat Exchanger (4) packet
Include the first import, first outlet, the second import and second outlet, first membrane distiller (5) includes that third import, third go out
Mouth and the 4th outlet, the described 4th of first membrane distiller (5) exports the described of the corresponding First Heat Exchanger (4)
Second import connects, the institute of first import and the first membrane distiller (5) described in its latter of the First Heat Exchanger (4)
State third outlet connection, the first outlet and the first membrane distiller (5) described in its latter of the First Heat Exchanger (4)
The third import connection, the second outlet and the First Heat Exchanger (4) described in its latter of the First Heat Exchanger (4)
The second import connection；
Second heat exchanger (2) include the 5th import, the 5th outlet, the 6th import and the 6th outlet, the 5th import with
Material liquid import connects, and the 6th outlet is connect with condensate outlet；
The third heat exchanger (3) include the 7th import, the 7th outlet, the 8th import and the 8th outlet, the 7th import with
5th outlet connection, the 8th outlet connects with the 6th import, the 7th outlet and are in the described in head end
The third import of one membrane distiller (5) connects；
Second membrane distiller (6) include the 9th import, the 9th outlet and the tenth outlet, the 9th import be in end
The first outlet of the First Heat Exchanger (4) connects, and the described 9th exports and be in First Heat Exchanger (4) described in end
The first import connection；
Tenth outlet passes through the vapour compression machine with the second outlet in First Heat Exchanger (4) described in end
(1) it is connect with the 8th import.
2. vacuum type multiple-effect membrane distillation system as described in claim 1, which is characterized in that the membrane component further includes
One gas-liquid separator (7), the gas-liquid separator include the 11st import, the 11st outlet and the 12nd outlet, the gas-liquid
The second outlet of the corresponding First Heat Exchanger (4) of the 11st import of separator connects, and the described 11st
Outlet is connect with second import of First Heat Exchanger (4) described in its latter, the institute in gas-liquid separator described in end
It states 11 outlets to connect with the 8th import by the vapour compression machine (1), the 12nd outlet and the condensate liquid
Outlet connection.
3. vacuum type multiple-effect membrane distillation system as claimed in claim 2, which is characterized in that the membrane component further includes
Two solution pumps (8), second solution pump (8) are set to first entrance.
4. vacuum type multiple-effect membrane distillation system as claimed in claim 3, which is characterized in that the membrane component further includes
Two material liquid tanks (9), described second material liquid tank (9) one end are connect with second solution pump (8), the other end corresponding described
The third outlet connection of one membrane distiller (5).
5. vacuum type multiple-effect membrane distillation system as claimed in claim 2, which is characterized in that further include the second gas-liquid separator
(10), the gas-liquid separator include the tenth triple feed inlet, the 13rd outlet and the 14th outlet, the tenth triple feed inlet respectively with
In gas-liquid separator described in end it is described 11 outlet and it is described tenth outlet connection, it is described 14th outlet with it is described cold
Condensate outlet connects.
6. vacuum type multiple-effect membrane distillation system as described in claim 1, which is characterized in that further include the first solution pump (11),
First solution pump (11) is set to the 7th exit.
7. vacuum type multiple-effect membrane distillation system as claimed in claim 4, which is characterized in that further include the first material liquid tank (12),
First material liquid tank (12) include the 15th import, the 15th outlet and the 16th import, the 15th import be in
The third outlet connection of first membrane distiller (5) described in head end, the 15th outlet are connect with the 7th import, institute
The 16th import is stated to connect with the 5th outlet.
8. vacuum type multiple-effect membrane distillation system as claimed in claim 7, which is characterized in that first material liquid tank (12) and institute
It states the second material liquid tank (9) and is equipped with heating device.
9. vacuum type multiple-effect membrane distillation system as described in claim 1, which is characterized in that the vapour compression machine (1) be from
Heart compressor or helical-lobe compressor.
10. the vacuum type multiple-effect membrane distillation system as described in any one of claim 1-9, which is characterized in that the film steams
It is two to evaporate component.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108176231A (en) * | 2018-03-08 | 2018-06-19 | 中国科学院理化技术研究所 | A kind of vacuum type multiple-effect membrane distillation system |
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