CN106365227B - Double latent multiple stage circulation membrane distillation methods and system - Google Patents
Double latent multiple stage circulation membrane distillation methods and system Download PDFInfo
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- CN106365227B CN106365227B CN201510441216.6A CN201510441216A CN106365227B CN 106365227 B CN106365227 B CN 106365227B CN 201510441216 A CN201510441216 A CN 201510441216A CN 106365227 B CN106365227 B CN 106365227B
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Abstract
The present invention is in relation to a kind of double latent multiple stage circulation membrane distillation methods and system, wherein using at least two pairs of latent membrane component series connection, heating steam passes sequentially through between each component metal tube and putamina, hot material liquid passes sequentially through between each component hydrophobic membrane silk and metal tube, and secondary steam passes sequentially through inside each component hydrophobic membrane silk.Secondary steam using upper level is condensed into product collection as between putamina and metal tube, exchanging heat with material liquid evaporation process in the heating steam to membrane module of next level assembly.Effective combination of membrane distillation evaporation process and heating Condensation, the condensation latent heat of heating steam just provides the evaporation latent heat demand of membrane distillation, avoid huge hot material flow quantity and the big hot material liquid temperature difference, the recycling of membrane distillation heat can efficiently be carried out, the efficiency of membrane distillation system can be greatly improved, membrane distillation operating cost is reduced.
Description
Technical field
The present invention relates to the membrane distillation method of water treatment field and systems, steam more particularly to a kind of double latent multiple stage circulation films
Evaporate method and system.
Background technique
The physical methods such as membrane separation process, the way of distillation can effective desalination, but membrane separation process film is expensive, to pretreatment
It is required that it is high, and there are problems that the serious wasting of resources and secondary pollution；The nothing in high-salt sewage can be recycled using the way of distillation
Machine salt, but equipment investment is huge, and operating cost is higher.Membrane distillation (Membrane Distillation, MD) is a kind of using thin
Water microporous barrier is Conventional espresso technique and membrane separation technique using film two sides vapor pressure differential as the membrane separating process of mass transfer driving force
A kind of liquid separation technology combined.During membrane distillation, dewatering microporous film does not participate in centrifugation directly, unique
Effect be exactly the barrier alternate as two, selectivity determined completely by vapour-liquid equilibrium.The mass transport process of membrane distillation generally comprises
The following three steps: being evaporated at the vapour-liquid interface of hot-fluid side；Steam molecule is transmitted by hydrophobic membrane micropore；Steam is in low temperature side
It condenses (or being pulled away).Compared with other separation processes, membrane distillation has rejection height, operation temperature than traditional distillation
It is low, operating pressure is low, can handle the advantages that high-concentration waste water；However the energy consumption height of membrane distillation is still and hinders the main of its development
Factor at present has much multiple-effect, the design of efficient membrane distillation technique method and system, and identical point is all to generate to membrane distillation
Secondary steam be recycled, be used to the heat of condensation release to heat material liquid, recycle the material liquid itself of heat
The evaporation of temperature drop progress membrane distillation.This may be to carry out inside film group device using the process of steam condensation heating material liquid,
It may also be carried out outside film group device.
Application No. is the patent applications of a kind of heat reclamation type pressure reducing film distillation assembly apparatus of 200810053905.x and method
Disclose be alternatively arranged by multiple groups, the frame membrane component unit that is serially connected and frame heat exchanger assembly form.Hot material liquid
The steam evaporated in membrane component unit condenses on heat exchanger assembly, and achievees the purpose that improve efficiency.
It discloses in component and fills out application No. is the patent application of 200910170615.8 heat recuperating membrane distillation apparatus and system
Fill breathable membrane distillation hydrophobic membrane and air-locked heat exchange membranes, hydrophobic membrane runs hot material liquid, heat exchange membranes operation when operation
The steam of cold burden liquid, the distillation of hot material liquid film can condense in the solid wall heat exchange membranes of cold burden liquid, and achieve the purpose that improve efficiency.
Solid wall heat exchange membranes, the non-porous fine and close hollow fibre filament of high molecular material preparation.Water and steam can not all pass through, and can carry out heat
It exchanges but heat transfer loss is big, rate of heat transfer is slow, and heat-transfer effect is poor.
Application No. is the patent applications of 201210072721.4 multiple-effect distillation devices and method to disclose offer of the present invention
A kind of multiple-effect distillation device and method.Distilling apparatus includes main evaporation zone, multiple-effect evaporation area；Wherein: main evaporation zone setting follows
Annular groove and main evaporation zone membrane component, circulating slot outlet connection main evaporation zone membrane component tube-side inlet, main evaporation zone
The tube side outlet connection circulating slot entrance of membrane component；At least one level heat exchange distilling apparatus is set in multiple-effect evaporation area, it is each
Grade heat exchange distilling apparatus includes membrane component and heat exchanger, above-mentioned every level-one membrane component and heat exchanger sequentially tube side string
Join, shell side is in parallel between membrane components at different levels.The present invention proposes multiple-effect membrane distillation method, by the water vapour during membrane distillation
Condensation is coupled with raw water heating process, recycles the heat of transformation of vapor during membrane distillation.
Frame component can not accomplish the combination evaporated and condensed, and be had according to the temperature and vacuum degree of evaporating principle steam
Evaporation liquid is closed and is lower than, the efficiency of system process disclosed in patent application 200810053905.x is also extremely low.
Pillar hydrophobic membrane and heat exchange membranes mixed packing, the method for operation disclosed in patent application 200910170615.8
Also do not accomplish the combination evaporated and condensed.If heat exchange Si Neitong steam, cavity leads to hot material liquid, takes out and steams inside hydrophobic membrane
Vapour, theoretically can accomplish the combination of evaporation with condensation reluctantly, but pressure drop of the steam in longer, relatively fine film wire
Can be bigger, and high molecular heat loss can be bigger, and this structure heat exchange silk quantitative proportion very big will could provide enough
Heat exchange and uniform thermal environment, and heat exchange silk ratio is excessive will lead to effective membrane area and reduce, and above situation can all be led
Cause whole efficiency low.
The disclosed water vapour condensation and raw water heating process by during membrane distillation of patent application 201210072721.4
Coupling, the heat demand of membrane distillation evaporation process are still to reduce to provide by the temperature of hot material liquid itself, and membrane efficiency is very low.
The energy regenerating of system in the case where " effect number " is unlimited, that is, cost of investment it is infinitely great in the case where, the energy consumption relative to evaporation
It is only capable of reduction by 50%.
In conclusion the research of membrane distillation is very more at present, the secondary steam generated to membrane distillation is mostly used to return greatly
It receives and utilizes, be used to the heat of secondary steam condensation release to heat material liquid, the temperature drop of the material liquid itself of heat is recycled to carry out
The evaporation process of membrane distillation, however due to the enlarge-effect of component, the thermal effect of the method for this heat recovery and utilization after amplification
Rate is extremely low, and consumption energy is high, limits the industrial application of membrane distillation.
Summary of the invention
In view of defect present in the above-mentioned prior art, the object of the present invention is to provide a kind of double latent multiple stage circulations
Membrane distillation method and system make it improve efficiency, reduce energy consumption, are applicable to industrial applications.
To achieve the goals above, a kind of double latent multiple stage circulation membrane distillation methods proposed according to the present invention, wherein using
At least two pairs of latent membrane component series connection, heating steam pass sequentially through between each component metal tube and putamina, and hot material liquid is successively
By the way that between each component hydrophobic membrane silk and metal tube, secondary steam is passed sequentially through inside each component hydrophobic membrane silk.
The present invention also can be used following technical measures and further realize.
Double latent multiple stage circulation membrane distillation methods above-mentioned, wherein the secondary steam warp that the first order membrane component generates
After vapour compression machine improves temperature and pressure, it is input in first order membrane component as heating steam to hot material liquid and conducts heat.
Double latent multiple stage circulation membrane distillation methods above-mentioned, wherein the secondary steam warp that any level membrane component generates
After vapour compression machine improves temperature and pressure, it is input in its membrane component as heating steam to hot material liquid and conducts heat.
Double latent multiple stage circulation membrane distillation methods above-mentioned, exclude wherein the heating steam is condensed into water from condensate outlet
Afterwards, it is exchanged heat by heat exchanger with the feed liquid that will enter feed liquid port, to preheat feed liquid.
Double latent multiple stage circulation membrane distillation methods above-mentioned, wherein the feed liquid inlet amount is 10L/min-300L/min, it is excellent
Select 100L/min-150L/min.
Double latent multiple stage circulation membrane distillation methods above-mentioned, wherein system vacuum is that 0.01MPa-0.099MPa is preferred
0.05MPa-0.09MPa。
Double latent multiple stage circulation membrane distillation methods above-mentioned, wherein feed liquid feeding temperature is 40 DEG C -99 DEG C, preferably 70 DEG C -90
℃。
To achieve the goals above, a kind of double latent multiple stage circulation membrane distillation systems proposed according to the present invention, including N
A double latent membrane components, dense feed liquid storage tank, feed liquid storage tank, pure water tank and heat exchanger, circulating pump, vacuum pump；N is more than or equal to 2；
Double latent membrane components are connected in series, and first order membrane component heating steam inlet connects supply steam, and first order film steams
The pure water tank that component condensate outlet tape splicing has vacuum pump is evaporated, first order membrane component feed liquid port is connected by raw water supply pump
Splicing liquid storage tank, first order membrane component material liquid outlet connect second level membrane component feed liquid port；First order membrane distillation group
The outlet of part secondary steam connects second level membrane component heating steam inlet；N grades of membrane component heating steam inlets connect
N-1 grades of membrane component secondary steam outlets, every level-one membrane component condensate outlet tape splicing in addition to the first order have vacuum
The pure water tank of pump, N grades of membrane component material liquid outlets connect dense feed liquid storage tank, and N grades of membrane component feed liquid ports meet N-1
Grade membrane component material liquid outlet, N grades of membrane component secondary steam outlets connect heat exchanger and are followed by the pure water with vacuum pump
Tank.
The present invention also can be used following technical measures and further realize.
Preceding double latent multiple stage circulation membrane distillation system, wherein the heat exchanger of connection feed liquid port with connect changing for condensate outlet
Hot device is same heat exchanger, can be by the heat transfer of condensed water to feed liquid.
Double latent multiple stage circulation membrane distillation systems above-mentioned, wherein further including steam generator, the supply steam is by steam
Generator provides.The present invention has obvious advantages and beneficial effects compared with the existing technology.By above-mentioned technical proposal, this hair
Bright double latent multiple stage circulation membrane distillation methods and system, at least have the advantage that
One, double latent multiple stage circulation membrane distillation methods of the invention and system, using the secondary steam of upper level as next
It in the heating steam to membrane module of level assembly between putamina and metal tube, exchanges heat with material liquid evaporation process, is condensed into product receipts
Collection.Effective combination of membrane distillation evaporation process and heating Condensation, the condensation latent heat for heating steam just provide film steaming
The evaporation latent heat demand evaporated avoids huge hot material flow quantity and the big hot material liquid temperature difference, can efficiently carry out membrane distillation
The recycling of heat can greatly improve the efficiency of membrane distillation system, reduce membrane distillation operating cost.
Two, double latent multiple stage circulation membrane distillation methods of the invention and system, it is possible to reduce prior art heat recovery system
Multiple groups equipment investment reduces occupation area of equipment.
Three, double latent multiple stage circulation membrane distillation methods of the invention and system, table of the film wire accumulation of pollutants in hydrophobic film wire
Face, rather than inside hydrophobic film wire, it is easy to clean, the waste of hydrophobic film wire is effectively reduced.
Four, double latent multiple stage circulation membrane distillation methods of the invention and system, membrane module membrane area is big, and sealing is tight, manufacture
It is at low cost.
Detailed description of the invention
Fig. 1 is the membrane component schematic diagram of double latent multiple stage circulation membrane distillation methods and system preferred embodiment of the invention.
Fig. 2 is that double latent multiple stage circulation membrane distillation methods of the invention and the membrane component cross section of system preferred embodiment show
It is intended to.
Fig. 3 is the membrane distillation system schematic of double latent multiple stage circulation membrane distillation methods and system preferred embodiment of the invention.
1 secondary steam exports 10 heat exchangers
2 material liquid outlet, 11 circulating pump
3 condensate outlet, 12 vacuum pump
The 4 dense feed liquid storage tanks of hydrophobic film wire 13
5 heating steam inlet, 14 feed liquid storage tank
6 metal tube, 15 pure water tank
7 putamina, 16 steam generator
8 feed liquid ports
Specific embodiment
It is of the invention to reach the technical means and efficacy that predetermined goal of the invention is taken further to illustrate, below in conjunction with
Attached drawing and preferred embodiment, to double latent multiple stage circulation membrane distillation methods proposed according to the present invention and its specific embodiment party of system
Formula, step, structure, feature and its effect are described in detail.
The invention mainly relates to following technical terms:
Membrane distillation: forming gas-liquid interface using miillpore filter, by picking dynamic progress liquid evaporation and volatile-resistant substance point
From process.
Hydrophobic film wire: a kind of hollow fiber film thread makes film that hydrophobicity, liquid water be presented by special material and technique
It will not pass through, steam can pass through, and realize membrane distillation process.
Sensible heat: the heat exchanged when temperature is raised and lowered in liquid, such as every kilogram of water be raised and lowered exchanged at 1 degree it is aobvious
Heat is 4.2kJ.
Latent heat: the heat that liquid evaporation or steam exchange when condensing, under equal conditions quantity is identical for the two.Every kilogram of water
The latent heat of evaporation is 2300kJ or so, is 550 times of sensible heat or so, i.e., needs 550 kilograms of water to reduce to one kilogram of water of evaporation
Once or 55 kilograms of water reduce by 10 degree, or one kilogram of steam of condensation.
Double latent membrane components: hollow fiber film thread is seated in metal tube by a kind of membrane module structure, the quantity of film wire
It depends on the circumstances, such metal tube is seated in putamina, metal tube quantity depends on the circumstances, and forms set by metal tube and film wire
Pipe, metal tube form the membrane component of the structure of array in putamina.
It has been investigated that existing film distillation technology is all the heat transfer type of " sensible heat-latent heat-sensible heat ".In capillary-pipe film
Hot strong brine is flowed, by the cooling of itself, provides heat to steam is flashed to by film, steam comes capillary-pipe film and metal
Cold metal tube is contacted between pipe is cooled into water, and the cooling water between metal tube and putamina will be taken away by the heating of itself
These heats；The prior art is all by the Condensation of membrane distillation process and feed liquid warm or material liquid heating process
Integrated, membrane distillation process has been completed in fact, is not combined effectively with condensation process, the still film group either inside membrane module
Outside part, energy utilization all can not be effectively carried out.A large amount of latent heat of condensation for preheating, can not high efficiente callback because
A large amount of cold burden liquid sensible heat is needed to receive the latent heat of this some vapor condensation.In addition, required a large amount of latent when the evaporation of membrane distillation
Heat is only provided by the temperature drop sensible heat of the hot material liquid itself of outside heating, same inefficiency.This technical method will not steam
Hair latent heat effectively combined with condensation latent heat, efficiency is low, be its can not industrial applications basic reason.
Illustrate below by theoretical calculation using the treatment process ratio of " latent heat-latent heat " using " sensible heat-latent heat-is aobvious
The treatment process of heat " has higher efficiency.
" sensible heat-latent heat-sensible heat " treatment process theory water yield:
If flowing 70 DEG C of the strong brine of 1kg/h in capillary-pipe film；Vacuum degree is 0.08MPa, and temperature drops to 60 DEG C
Flux is zero, does not consider the resistance of film itself, 4.2kJ/kg* DEG C of the specific heat of water, and the heat of vaporization of water is averaged 2300kJ/kg, then is
The theoretical maximum water yield of system are as follows:
4.2kJ/kg* DEG C of * 1kg/h* (70 DEG C -60 DEG C)/2300kJ/kg=0.018kg/h
" latent heat-latent heat " treatment process theory water yield:
If flowing 70 DEG C of the strong brine of 1kg/h between hydrophobic film wire and metal tube；Vacuum degree 0.08MPa, this side
Strong brine temperature will not reduce in method, not consider the resistance of film itself, and the heat of vaporization of water is averaged 2300kJ/kg, then the reason of system
By maximum water yield are as follows:
2300kJ/kg*1kg/h/2300kJ/kg=1kg/h
In conclusion it is " sensible heat-latent heat-sensible heat " that the limit theory efficiency ratios of two methods, which are " latent heat-latent heat ",
55.5 times, can sharply decline in practice as the water yield of the reduction film of temperature, thus overall efficiency ratio can gap it is bigger.
In the process of " sensible heat-latent heat-sensible heat ", strong brine is reduced by temperature after membrane module, it is necessary to
Reheating is returned, and needing heat is [4.2kJ/kg* DEG C of * 1kg/h* (70 DEG C -60 DEG C)]=42kJ/h；Cooling water passes through itself
Heat has been taken away in heating will also discharge, but the temperature of cooling water is too low, so can only substantially be discharged in air." latent heat-is latent
In the process of heat ", temperature does not change after strong brine passes through membrane module, does not need additionally to heat；Origin of heat is that film steams
The condensation for evaporating the newborn secondary steam of component provides, so demand to cooling water also very little, is discharged to the heat wasted in air
Also very little.The performance study of film has been able to obtain the biggish film of water yield at present, but is applied to component, in system
When it is very low with regard to efficiency, main cause is exactly the congenital limitation of " sensible heat-latent heat-sensible heat " this heat-transferring method.The present invention
The technique carried out simultaneously using " latent heat-latent heat ", when heating steam is cooled between putamina 7 and metal tube 6 and forms condensation
While water, heat transfer just makes the water evaporation in feed liquid to the feed liquid between metal tube 7 and hydrophobic film wire 4, these heats
Hydrophobic film wire 4 is penetrated at secondary steam, membrane module is extracted out of hydrophobic film wire 4, evaporation latent heat during membrane distillation can be made
It is effectively combined with condensation latent heat, and is utilized by improving secondary steam temperature and pressure as heating steam circulation, greatly dropped
Low membrane distillation energy consumption.
Refering to Figure 1, being the membrane distillation of double latent multiple stage circulation membrane distillation methods and system preferred embodiment of the invention
Component diagram.Membrane component has putamina 7, secondary steam outlet 1 is provided on putamina 7, material liquid outlet 2, condensate liquid go out
Mouthful 3, heating steam inlet 5, feed liquid port 8 are provided with metal tube 6 in putamina 7, and the axis of metal tube 6 and the axis of putamina 7 are flat
It goes, end cap certain distance is welded with two metallic porous sheets to distance up and down in putamina 7, and 6 both ends outer edge of metal tube and metal are more
Orifice plate welded seal forms two parts insulating space outside metal tube inside and metal tube；Filling is variable amount of in metal tube 6 dredges
Moisture film silk 4, hydrophobic 4 axis of film wire is parallel with 6 axis of metal tube, and hydrophobic film wire 4 is slightly longer than metal tube 6, and hydrophobic 4 lower end of film wire is adopted
It is poured with sealing technology and is sealed in putamina lower cover, upper end pours at a certain distance from apart from putamina upper end cover, in hydrophobic film wire 4
It is interior between upper end cover formed intercommunication space, putamina 7, metal tube 6 and 4 three of hydrophobic film wire it is mutual before positional relationship such as
Shown in Fig. 2；The confined space composition heating formed between heating steam inlet 5, condensate outlet 3, putamina 7 and metal tube 6 is steamed
Vapour access；The confined space composition processing feed liquid formed between feed liquid port 8, material liquid outlet 2, metal tube 6 and hydrophobic film wire 4 is logical
Road；Secondary steam outlet 1,4 inner space of hydrophobic film wire form secondary steam access.It is preferred that putamina 7 is cylinder type, metal tube
6 in putamina 7 array distribution, hydrophobic 4 upper and lower ends of film wire using sealing technology seal.
Hydrophobic film wire 4 is preferably dimensioned to be diameter 0.1mm -10m, length 0.1mm-10m；
The thickness of putamina 7 is preferably 0.1mm-1m；
Metal tube 6 diameter 0.1mm-10m, length 0.1mm-10m；
The quantity of 7 inner metal tube 6 of putamina is preferably 1-100000 root；
The quantity of 6 internal drainage film wire of metal tube is preferably 1-1000000 root；
The sealing thickness of hydrophobic film wire 4 is preferably 0.1mm -1m.
7 material of putamina include but is not limited to the metals such as PVC, ABS, stainless steel, PPR, cast iron, aluminium alloy, titanium alloy, copper or
The single material or multiple combinations of plastics.
The material of metal tube 6 includes but is not limited to the single material or a variety of such as stainless steel, cast iron, aluminium alloy, titanium alloy, copper
Combination.
The material of hydrophobic film wire 4 includes but is not limited to polyether sulfone, polysulfones, Kynoar, polyvinyl chloride, cellulose, gathers
The single material such as amide, polypropylene, polyethylene, polytetrafluoroethylene (PTFE) or multiple combinations.
It please refers to shown in Fig. 3, is the membrane distillation of double latent multiple stage circulation membrane distillation methods and system preferred embodiment of the invention
System schematic.The system includes at least two pairs of latent membrane components, and each membrane component is referred to as level-one, and first order film steams
It evaporates component heating steam inlet 1 and connects supply steam, 3 tape splicing of condensate outlet has the pure water tank 15 of vacuum pump；8 splicing of feed liquid port
Liquid circulating pump 11 or feed liquid storage tank 14, material liquid outlet 2 connect second level membrane component feed liquid port 8；Secondary steam outlet 1 connects the
Second level membrane component heating steam inlet 5；Second level membrane component heating steam inlet 5 connects first order membrane component two
Secondary steam (vapor) outlet 1,3 tape splicing of condensate outlet have the pure water tank 15 of vacuum pump 12；Feed liquid port 8 connects first order membrane component material
Liquid outlet 2, material liquid outlet 2 connect third level membrane component feed liquid port 8, and secondary steam outlet 1 connects third level membrane component
Heating steam inlet 5；N-th grade of membrane component heating steam inlet 5 connects the (n-1)th effect membrane component secondary steam outlet 1, cold
3 tape splicing of condensate outlet has the pure water tank 15 of vacuum pump 12, and feed liquid port 8 connects (n-1)th grade of membrane component material liquid outlet 2, feed liquid
Outlet 2 connects (n+1)th grade of membrane component feed liquid port 8, and secondary steam outlet 1 connects (n+1)th grade of membrane component heating steam and enters
Mouth 5；Final stage membrane component heating steam inlet 5 connects level-one membrane component secondary steam outlet 1, and condensate outlet 3 connects
Pure water tank 15 with vacuum pump 12, feed liquid port 8 connect upper level membrane component material liquid outlet 2, and 2 splicing of material liquid outlet is dense
Contracting liquid storage tank 13, secondary steam outlet 1 connect heat exchanger and the pure water tank 15 with vacuum pump 12.
When system stable operation, strong brine enters first order membrane component feed liquid port 8 by circulating pump 11, and heating is steamed
Vapour is entered between first order membrane component metal tube 6 and putamina 7 by heating steam inlet 5, is conducted by 6 heat of metal tube
Hot material liquid is given, steam is condensed into condensed water and enters the pure water tank 15 with vacuum pump, and hot material liquid is in hydrophobic film wire 4 and metal tube 6
Between pass through the heating of steam, carry out membrane distillation process, part solution is gasificated into steam by hydrophobic 4 fenestra of film wire into hydrophobic
Inside film wire 4, remaining concentrated solution enters next stage membrane component, and the steam in hydrophobic film wire 4 passes through under the action of vacuum
The heating steam inlet 5 that secondary steam outlet 1 is discharged into second level membrane component carries out condensation next time, or by steaming
Enter the condensation of the progress of heating steam inlet 5 of second level membrane component next time after the processing of vapour compressor 9；Into
The concentrated solution of second level membrane component carry out secondary membrane distillation process generate some vapor by inside hydrophobic film wire 4 to two
Secondary steam (vapor) outlet 1 enters back into the heating steam inlet 5 of next stage membrane component, repeatedly, every level-one membrane component
Feed liquid is all heated by the evaporation evaporated vapor of upper level membrane component, carries out membrane distillation process, has the solution of part to flash to
Steam becomes the heating steam of next stage membrane component, and the heating steam of every level-one membrane component can condense after the heat exchange
Recyclable at pure water, the evaporation process and condensation process of every level-one membrane component are all to occur simultaneously.It thus will be in feed liquid
Water extract, solute is concentrated.
Embodiment one:
Double 3 grades of membrane distillation systems of diving, membrane module Φ 200mm*500mm, 105 DEG C of initial heating steam, feed liquid feeding temperature
90 DEG C, input concentration 6%, concentration 18% after concentrated water concentration, inlet amount 120L/min, an effect membrane module vacuum degree 0.05MPa, two
Imitate membrane module vacuum degree 0.07MPa, triple effect membrane module vacuum degree 0.09MPa.
Embodiment two:
Double 5 grades of membrane distillation systems of diving, membrane module Φ 200mm*500mm, 105 DEG C of initial heating steam, feed liquid feeding temperature
90 DEG C, input concentration 6%, concentration 18% after concentrated water concentration, inlet amount 120L/min, an effect membrane module vacuum degree 0.04MPa, two
Imitate membrane module vacuum degree 0.052MPa, triple effect membrane module vacuum degree 0.064MPa, quadruple effect membrane module vacuum degree 0.076MPa, five effects
Membrane module vacuum degree 0.09MPa.
Embodiment three:
Double 5 grades of membrane distillation systems of diving, membrane module Φ 200mm*500mm, 105 DEG C of initial heating steam, feed liquid feeding temperature
90 DEG C, input concentration 6%, concentration 18% after concentrated water concentration, inlet amount 150L/min, an effect membrane module vacuum degree 0.04MPa, two
Imitate membrane module vacuum degree 0.052MPa, triple effect membrane module vacuum degree 0.064MPa, quadruple effect membrane module vacuum degree 0.076MPa, five effects
Membrane module vacuum degree 0.09MPa.
Example IV:
Double 5 grades of membrane distillation systems of diving, membrane module Φ 200mm*500mm, 105 DEG C of initial heating steam, feed liquid feeding temperature
90 DEG C, input concentration 6%, concentration 18% after concentrated water concentration, inlet amount 120L/min, an effect membrane module vacuum degree 0.03MPa, two
Imitate membrane module vacuum degree 0.045MPa, triple effect membrane module vacuum degree 0.06MPa, quadruple effect membrane module vacuum degree 0.075MPa, five effects
Membrane module vacuum degree 0.09MPa.
Embodiment five:
Double 5 grades of membrane distillation systems of diving, membrane module Φ 200mm*500mm, 105 DEG C of initial heating steam, feed liquid feeding temperature
95 DEG C, input concentration 6%, concentration 18% after concentrated water concentration, inlet amount 120L/min, an effect membrane module vacuum degree 0.04MPa, two
Imitate membrane module vacuum degree 0.052MPa, triple effect membrane module vacuum degree 0.064MPa, quadruple effect membrane module vacuum degree 0.076MPa, five effects
Membrane module vacuum degree 0.09MPa.
Double latent multiple stage circulation membrane distillation system test results of the invention are as shown in table 1:
1 pair, table latent multiple stage circulation membrane distillation system test result:
| Membrane distillation system | Embodiment one | Embodiment two | Embodiment three | Example IV | Embodiment five |
| Average flux (LMH) | 12.5 | 13.2 | 13.8 | 12.9 | 14.1 |
| System water yield (ton/d) | 1.8 | 3.17 | 3.31 | 3.10 | 3.38 |
| System water generation ratio (ton steam/ton water) | 0.35 | 0.22 | 0.21 | 0.23 | 0.19 |
| Comprehensive energy consumption (Kwh/ tons of water) | 34.3 | 21.56 | 20.58 | 22.54 | 18.62 |
This pair of latent multistage membrane distillation method and system, using double latent membrane components, combination multiple-effect process.The system
Evaporation latent heat during membrane distillation can be made effectively to be combined with condensation latent heat, membrane distillation energy consumption can be greatly reduced, theoretical energy consumption is
The 1/n of evaporation, n are " series ".Such as the double latent array type Multistage Membranes Distallation systm theoretical energy consumptions of Pyatyi are the 1/5 of evaporation, that is, are dropped
Low 80% energy consumption.Double latent array type Multistage Membranes Distallation systms and its method of operation, the secondary steam of upper level is as next stage
Heating steam, condensation latent heat recycling with evaporation latent heat supply couples.Using double latent array type multistage membrane components；Putamina 7
The operation heating steam between metal tube 6；Feed liquid is run between metal tube 6 and hydrophobic film wire 4；Operation evaporation in hydrophobic film wire 4
Steam.
Although the present invention has been disclosed as a preferred embodiment, it is so not intended to limit the invention the range of implementation, foundation
Simple equivalent changes and modifications, still fall within technical solution of the present invention made by claims of the present invention and description
In range.
Claims (7)
1. a kind of double latent multiple stage circulation membrane distillation methods, it is characterised in that using at least two pairs of latent membrane component series connection, add
Hot steam passes sequentially through between each component metal tube and putamina, hot material liquid pass sequentially through each component hydrophobic membrane silk and metal tube it
Between, secondary steam passes sequentially through inside each component hydrophobic membrane silk, and the feed liquid inlet amount is 100L/min-150L/min, system
Vacuum degree is 0.05MPa-0.09Mpa, and the feed liquid feeding temperature is 70 DEG C -90 DEG C.
2. double latent multiple stage circulation membrane distillation methods according to claim 1, it is characterised in that first order membrane component is raw
At secondary steam after vapour compression machine improves temperature and pressure, be input in first order membrane component as heating steam
It conducts heat to hot material liquid.
3. double latent multiple stage circulation membrane distillation methods according to claim 1, it is characterised in that any level membrane component is raw
At secondary steam after vapour compression machine improves temperature and pressure, be input in its membrane component as heating steam to heat
Feed liquid heat transfer.
4. double latent multiple stage circulation membrane distillation methods according to any one of claims 1 to 3, it is characterised in that heating steam is cold
Water is congealed into after condensate outlet exclusion, is exchanged heat by heat exchanger with the feed liquid that will enter feed liquid port, to preheat
Feed liquid.
5. a kind of double latent multiple stage circulation membrane distillation systems, it is characterised in that including N number of double latent membrane components, dense feed liquid storage tank,
Feed liquid storage tank, pure water tank and heat exchanger, circulating pump, vacuum pump；N is more than or equal to 2；Double latent membrane components are connected in series,
First order membrane component heating steam inlet connects supply steam, and first order membrane component condensate outlet tape splicing has vacuum pump
Pure water tank, first order membrane component feed liquid port is by raw water supply pump binder liquid storage tank, first order membrane component
Material liquid outlet connects second level membrane component feed liquid port；The outlet of first order membrane component secondary steam connects second level membrane distillation
Component heating steam inlet；N grades of membrane component heating steam inlets connect N-1 grades of membrane component secondary steam outlets,
Every level-one membrane component condensate outlet tape splicing in addition to the first order has the pure water tank of vacuum pump, N grades of membrane component material
Liquid outlet connects dense feed liquid storage tank, and N grades of membrane component feed liquid ports connect N-1 grades of membrane component material liquid outlets, N grades of films
The outlet of distillation component secondary steam is followed by the pure water tank with vacuum pump by heat exchanger.
6. double latent multiple stage circulation membrane distillation systems according to claim 5, it is characterised in that the first level assembly feed liquid of connection
The heat exchanger of entrance is same heat exchanger with the heat exchanger for connecting N grades of condensate outlets, can be by the heat transfer of condensed water extremely
Feed liquid.
7. double latent multiple stage circulation membrane distillation systems according to claim 5 or 6, it is characterised in that further include steam generation
Device, the supply steam are provided by steam generator.
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| CN106865663A (en) * | 2017-03-30 | 2017-06-20 | 中建安装工程有限公司 | Energy-saving Membrane Materials wastewater treatment equipment and method that a kind of modularization is installed |
| CN108211801A (en) * | 2018-03-07 | 2018-06-29 | 北京天地人环保科技有限公司 | A kind of multiple-effect distillation device, system and method |
| CN110170235A (en) * | 2019-06-14 | 2019-08-27 | 华中农业大学 | The double film heat exchangers of hydrophobe strengthen the CO of waste heat recycling2Chemical absorbing System and method for |
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