CN103193295A - Immersed dissolved gas vacuum membrane distillation water processing method - Google Patents
Immersed dissolved gas vacuum membrane distillation water processing method Download PDFInfo
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Abstract
The invention relates to an immersed dissolved gas vacuum membrane distillation water processing method. The method comprises the following steps: immersing a distillation membrane distillation assembly in a heating water box, dissolving a gas in inlet water through adopting a gas dissolving pump, and effectively removing pollutants in the inlet water through vacuum membrane distillation in order to realize the separation and concentration of the pollutants in the inlet water. The method has the advantages of simple required equipment, uniform gas-liquid mixing, low energy consumption and cost, simple operation, good membrane pollution resistance and long running period. The method can effectively remove a large amount of salts, a small amount of COD and other pollutants in the wastewater, reduce the sewage discharge amount and realize the efficient utilization of a water resource when the method is used for processing reverse osmosis concentrated water of wastewater generated in the production of an olefin polymerization catalyst.
Description
Technical field
The present invention relates to water treatment and membrane separation technique field, specifically, the present invention relates to a kind of immersion air-dissolved vacuum membrane distillation treatment process of reverse osmosis concentrated water, more particularly, the air-dissolved vacuum membrane distillation that the present invention relates to a kind of reverse osmosis concentrated water of petrochemical enterprises is handled reuse method.
Background technology
In recent years, in order to respond the call of national energy-saving and emission-reduction, petroleum chemical enterprise's waste water adopts the two membrane process of ultrafiltration/reverse osmosis to carry out reuse after the advanced treatment more, has satisfied the water demand of production upstream technology substantially.Yet consequent reverse osmosis concentrated water becomes one and handles a difficult problem, and this strand waste water can not discharge can not reuse, brings great puzzlement for each enterprise.
Membrane distillation be owing to can remove the salinity of greater concn and higher ratio of desalinization and be subjected to the various countries expert gradually and pay attention to and launched broad research, it can be at last the highest membrane technique of desalting efficiency up to now, ratio of desalinization is up to more than 99%.Membrane distillation is to be the eighties in last century the hydrophobic membrane technology that sea water desalinization is researched and developed, and it is to adopt microporous hydrophobic membrane, is a kind of new membrane sepn process of motivating force with film both sides steam pressure difference.
The used film of membrane distillation is not by the dewatering microporous film of pending solution-wet, namely has only steam can enter fenestra, and liquid can not see through fenestra.According to the difference of vapor diffusion to film cold side condensing mode, membrane distillation generally can be divided into four types: direct contact type membrane distillation (DCMD), GAP TYPE membrane distillation (AGMD), vacuum type membrane distillation (VMD), gas are swept formula membrane distillation (SGMD).Wherein VMD is the membrane process of constant temperature, and film sees through side and vacuumizes with vacuum pump, and to cause the bigger steam pressure difference in film both sides, the volatilization component is drawn the back condensation from cold side, and the heat conduction loss of this membrane distillation process is less, can ignore substantially.
Entrained gas is the method paid close attention to of this area in recent years in the feeding liquid of VMD process.Patent CN 101659451A relates to a kind of method for treating high-salt water by air stripping type membrane distillation, this method adopts the direct contact type membrane distillation of hollow fiber film assembly, sewage enters the film high-temp. side at the air formation biphase gas and liquid flow that raw water box heats by hydrothermal solution recycle pump and air compressor machine or blower fan generation, the membrane permeation side adopts recycle pump to circulate water of condensation and will see through steam and the condensation of gas of film and be transported to the product water tank, through the concentrate recirculation of film to raw water box.Plenum system is for to stop ram charging by the standard width of a room in an old-style house between magnetic valve, adopts the shortcoming of ram charging to be, and is bigger to the impact of film itself, and cause air water to mix inequality and the stripping effect discontinuous, the operation of inlet side is also impacted.
Patent CN 101664642A and document " research of air-blowing vacuum membrane still-process " (water technology, 2009,35 (12), 34～37) also relate to a kind of air-blowing vacuum membrane distillation apparatus and method, these apparatus and method adopt the vacuum membrane distillation of hollow fiber film assembly, the mode of vacuumizing is that inner pressed is that tube side vacuumizes, and sewage is walked in the tubular fibre fenestra.This method also blasts low-pressure compressed air and sewage formation biphase gas and liquid flow in hollow fiber film assembly ingress, and former water does not comprise wastewater from chemical industry, and does not limit operational condition.
In addition, patent CN1526650 relates to a kind of film distilling seawater desalination system of high-efficiency and low-cost, this patent is to connect the comparatively complicated frothing machine of a structure raising water loop, put as the micro bubble makeup, before this device, be provided with the gas under pressure supply, the preheating gas under pressure that this device provides and sea water mixing become to have the working liquid of high temperature, this working liquid is put by the micro bubble makeup and is carried out size degradation emulsification, the miniaturization that becomes because of a large amount of aerations of water molecules wherein, the relative quantity of steam that produces increases.This patent need be more with equipment, and structure is comparatively complicated, and operating process is complicated, and production cost is higher, and energy consumption is bigger, and the mould material pore size that adopts is 0.001～0.005 μ m.And the membrane distillation system for handling that patent CN1526650 provides is seawater.
Above-mentioned film distillation technology adopts is chlamydate hollow-fibre membrane, is the external placed type operation, although membrane distillation type difference, sewage is all walked in the tubular fibre fenestra, and the shell side of membrane module forms vacuum or condensation system.The shortcoming of this kind mode is because the film silk is thinner, causes dirtyly stifled easily in membrane module ingress and film silk, and the concentration polarization influence is bigger, form film easily and pollute, and the easy cleaning not of the membrane module after polluting.In addition, owing to adopt the external placed type operation, heat is partial loss in the pipeline course of conveying, and heat utilization ratio is low, and excessive tolerance causes the reduction of per-meate side vacuum tightness, the increase energy consumption easily.Above-mentioned patent all adopts air compressor machine or blower fan to blast air, the bubble that air compressor machine or blower fan produce is bigger, and enters membrane module after sewage mixes in pipeline, because pipeline limits, may cause gas dispersed bad in water, problem such as air water is mixed inhomogeneous.
What membrane distillation adopted is microporous hydrophobic membrane, and based on the mass transport mechanism of microporous hydrophobic membrane, the contamination resistance of membrane distillation is stronger, pollutes but also form film inevitably, and the pollution of the used microporous hydrophobic membrane of membrane distillation is mainly film surface pollution, and the fenestra internal contamination is less relatively.Because the handled lower high salt sewage of suspension content that generally is of membrane distillation, as systems such as reverse osmosis concentrated waters, therefore, the film of membrane distillation process pollutes and is mainly salt crystallization, fouling and the Organic pollutants that concentration polarization causes.So concentration polarization is a very significant effects factor in the membrane distillation process, avoid or reduce as far as possible.
Therefore, problem at present existence, need a kind of required equipment of exploitation simple, gas-liquid mixed is even, and heat conduction loss is few in the operational process, energy consumption is low, easy and simple to handle, both can well preventing membrane pollution, it is wetting to reduce film again, reduce the influence of concentration polarization and temperature difference polarization, the reverse osmosis concentrated water membrane distillation treatment technology in the cycle of operation of membrane component and prolong and work-ing life.
Summary of the invention
Technical problem to be solved by this invention is at above-mentioned the deficiencies in the prior art, and the molten gas vacuum membrane distillation of a kind of immersion water treatment method is provided.This method is immersed in the membrane distillation assembly in the heating water tank, adopts air dissolved pump to dissolve in gas simultaneously in feeding side waste water, removes pollutent in the dense water effectively by vacuum membrane distillation, realizes the separation of dense water pollutant and concentrates.This method required equipment is simple, and gas-liquid mixed is even, and energy consumption and cost are lower, and be easy and simple to handle, and the preventing membrane pollution performance is good, and the cycle of operation is long.For the treatment of the reverse osmosis concentrated water of olefin polymerization catalysis factory effluent, can effectively remove a large amount of salinities in the waste water, a small amount of COD and other pollutent, reduce quantity of wastewater effluent, realized the efficient utilization of water resources.
For this reason, the invention provides the molten gas vacuum membrane distillation of a kind of immersion water treatment method, comprising:
Steps A, water inlet are mixed formation influent gas liquid mixture with gas;
Step B, the influent gas liquid mixture enters heating water tank, is heated to the influent gas liquid mixture that preset temperature obtains preset temperature;
Step C vacuumizes the formation negative pressure in the side that sees through of membrane distillation assembly;
Step D is seeing through under the side vacuum action, the fenestra of the gas in the influent gas liquid mixture of preset temperature, steam permeable membrane distillation assembly, and seeing through side condensation formation membrane distillation product water;
Wherein, steps A is dissolved in into water formation influent gas liquid mixture by air dissolved pump with gas.
According to the inventive method, gas described in the steps A is nitrogen, oxygen or airborne a kind of or two kinds; The volume ratio of gas and liquid is 0.01: 1～0.5: 1 in the described influent gas liquid mixture.The volume ratio of gas and liquid is 0.08: 1～0.2: 1 in the preferred described influent gas liquid mixture.
According to the inventive method, water inlet described in the steps A comprises the reverse osmosis concentrated water from reverse osmosis system, high salt sewage, seawater etc., and described water inlet pH is 6.5～8.5, and preferred described water inlet pH is 7～8.
According to the inventive method, the liquid mixture of influent gas described in the step B enters heating water tank by air dissolved pump.
According to the inventive method, the preset temperature of the described water inlet of step B is 45～95 ℃.The preset temperature of preferred described water inlet is 65～85 ℃.
According to the inventive method, the assembly of membrane distillation described in the step C is immersed in the heating water tank.The assembly of membrane distillation described in the step C comprises tubular fibre curtain type film assembly or plate and frame module.The mould material of described membrane distillation assembly is polyvinylidene difluoride (PVDF), tetrafluoroethylene or microporous polypropylene membrane material.Wherein, the pore diameter range of described microporous membrane material is 0.1～0.5 μ m, and the pore diameter range of preferred described microporous membrane material is 0.15～0.22 μ m.
According to the inventive method, the seeing through wall pressure and be-0.01 of membrane distillation assembly among the step C～-0.1MPa.The seeing through wall pressure and be-0.085 of preferred described membrane distillation assembly～-0.1MPa.
According to the inventive method, behind the fenestra of the gas in the liquid mixture of influent gas described in the step D, steam permeable membrane distillation assembly, seeing through condensation formation membrane distillation product water under the side condenser effect.
According to the inventive method, the dense water of membrane distillation that the process of membrane distillation described in the step D produces regularly discharging focuses on.
The thermal source of membrane distillation system can adopt factory's low-temperature waste heat, exhaust steam heating or electrically heated among the present invention, or in order to cut down the consumption of energy, takes full advantage of peripheral used heat.According to the present invention, the control of the cycles of concentration of described vacuum membrane distillation system is about 5～7 times.Employing is according to the molten gas vacuum membrane distillation of the immersion of the inventive method system handles reverse osmosis concentrated water, and the operating flux scope of membrane distillation is 5～25L/m
2H, the membrane distillation ratio of desalinization is higher than 99%.
The essential distinction of the present invention and prior art is, the present invention relates to the molten gas vacuum membrane distillation of a kind of immersion water treatment method.Different with the immersion ultra-filtration process, the film of ultra-filtration process pollutes cake layer pollution that macromole such as being mainly suspended substance or large particulate matter cause, colloid pollution etc.Therefore, the immersion ultrafiltration is polluted for the macromole of removing or prevent suspended substance, colloid etc., and the aeration rate of requirement is bigger, and this just causes the fracture of wire phenomenon of membrane module in the immersion ultra-filtration process easily.And the handled lower high salt sewage of suspension content that generally is of membrane distillation process, as systems such as reverse osmosis concentrated waters, the film of membrane distillation process pollutes and is mainly salt crystallization, fouling and the Organic pollutants that concentration polarization causes.Therefore, the submerged membrane still-process mainly be for fear of or reduce concentration polarization and temperature difference polarization in the sewage, its required tolerance is less than the immersion ultrafiltration, and the present invention is referred to as molten gas, and lower tolerance suppresses or reduced fracture of wire phenomenon in the submerged membrane still-process; Simultaneously, less tolerance is not easy to cause the reduction of per-meate side vacuum tightness, therefore can cut down the consumption of energy.
Compare with conventional external placed type vacuum membrane distillation, water inlet and air can fully mix in heating water tank in the immersion vacuum membrane distillation process, gas-liquid mixed is more even, along with constantly concentrating of membrane distillation process, water inlet can in time fully be mixed, and has reduced the influence of concentration polarization and temperature difference polarization, reduced the film pollution, simultaneously, the immersion vacuum membrane distillation requires low to the water inlet pre-treatment, and can reduce the calorific loss in the pipeline course of conveying.
Compare with conventional vacuum membrane distillation, molten gas vacuum membrane distillation dissolves in gas in the hot side water inlet of vacuum membrane distillation, reduced steam partial pressure, be conducive to remove more impurity with littler transmembrane pressure, and make hot side form surface easier formation one deck air film, water and organic solvent have been weakened to the wetting influence of hydrophobic membrane, reduced the film pollution, and strengthened perturbation action in the water inlet, reduced steam condensing in fenestra simultaneously, prolong the cycle of operation of membrane module, improved the operating flux of film.
The present invention compares with patent CN 101659451A, and the present invention adopts vacuum membrane distillation, and the membrane distillation flux is higher, and heat conduction loss is littler; With patent CN 101659451A, CN101664642A and document " research of air-blowing vacuum membrane still-process " (water technology, 2009,35 (12)) compare, the present invention adopts air dissolved pump to dissolve in micro-bubble in water inlet, compare with the air that air compressor machine or blower fan produce, the present invention adopts air dissolved pump that gas is provided, can form littler, more uniform bubble, the micro bubble particle diameter that air dissolved pump produces is about 20～40 μ m, gas and liquid dissolved efficiency are up to 80～100%, the more abundant contact of gas-liquid two-phase has improved the membrane distillation flux, reduced the influence of concentration polarization and temperature difference polarization, reduce the film pollution, improved membrane distillation system recoveries rate, prolonged cleaning interval and the work-ing life of film.
Adopt the inventive method that reverse osmosis concentrated water is carried out degree of depth membrane distillation and handle, can take full advantage of the low grade heat energy of system's periphery, realize that the height of reverse osmosis concentrated water is recycled, to greatest extent the recycle-water resource; Therefore, particularly preferred, the processing object of the inventive method is mainly and is reverse osmosis concentrated water of petrochemical enterprises, this waste water saltiness height, and its concrete water quality situation sees Table 1.
Table 1 reverse osmosis concentrated water of petrochemical enterprises water quality
Through the reverse osmosis concentrated water after the inventive method processing, membrane distillation produces water power and leads≤3 μ S/cm, produces water COD
Mn＜3mg/L, the water rate of recovery is higher than 80%, and membrane distillation produces water and can be used as production technique water or de-salted water, has realized the utilization of high salt sewage recycling.
Description of drawings
Come the present invention is described in further detail below in conjunction with accompanying drawing:
Fig. 1 is the process flow diagram of embodiment 1～5
Fig. 2 is the process flow diagram of Comparative Examples 1
Fig. 3 is the process flow diagram of Comparative Examples 2
The implication of Reference numeral is as follows among Fig. 1 and Fig. 2: the molten gas vacuum membrane distillation of 1 immersion system; The non-molten gas vacuum membrane distillation of 1 ' immersion system; 2 liquid meters; 3 gas meters; 4 air dissolved pumps; 4 ' fresh feed pump; 5 heating water tank; 6 membrane distillation assemblies; 8 membrane distillation assemblies see through side; 9 condensers; 10 gas-liquid separators; 11 surge tanks; 12 vacuum pumps; 13 produce water pot; 14 water inlets; 15 gases; 16 influent gas liquid mixtures; The influent gas liquid mixture of 17 preset temperatures; The water inlet of 17 ' preset temperature; 18 water vapors and other gases; 19 membrane distillations produce water; The dense water of 20 membrane distillations.
" the non-molten gas vacuum membrane distillation of external placed type system that the implication of Reference numeral is as follows among Fig. 3: 1; 2 liquid meters; 4 " fresh feed pumps; 5 heating water tank; 6 membrane distillation assemblies; 7 membrane distillation component heat sides; 8 membrane distillation assemblies see through side; 9 condensers; 10 gas-liquid separators; 11 surge tanks; 12 vacuum pumps; 13 produce water pot; 14 water inlets; 17 " water inlet of preset temperature; 18 water vapors and other gases; 19 membrane distillations produce water; The dense water of 20 membrane distillations.
Embodiment
Describe the present invention in detail below in conjunction with embodiment and accompanying drawing, these embodiment and accompanying drawing only play the illustrative effect, are not limited to range of application of the present invention.
Among Fig. 1, pH be 6.5～8.5 water inlet 14 through liquid meter 2 metering backs with measure through gas meter 3 after gas 15 mix formation influent gas liquid mixture 16 by air dissolved pump 4 with 0.01: 1～0.5: 1 volume ratio, enter heating water tank 5 and be heated to preset temperature, the preset temperature that obtains is that 45～95 ℃ influent gas liquid mixture 17 enters the membrane distillation assembly 6 that is immersed in the heating water tank 5, the side 8 that sees through of membrane distillation assembly 6 is passed through vacuum pump 12 via condenser 9, gas-liquid separator 10 and surge tank 11 vacuumize formation-0.01～-negative pressure of 0.1MPa, seeing through under side 8 vacuum action, preset temperature is the gas in 45～95 ℃ the influent gas liquid mixture 17, the fenestra of steam permeable membrane distillation assembly 6 is seeing through side 8 formation water vapor and other gases 18, water vapor and other gas 18 are by condenser 9 condensations, and form membrane distillations through gas-liquid separator 10 and produce water 19 and enter and produce water pot 13, remove to use water spot then; The discharging regularly of the dense water 20 of membrane distillation focuses on.
Among Fig. 2, pH be 6.5～8.5 water inlet 14 after liquid meter 2 meterings by fresh feed pump 4 ' enter heating water tank 5 to be heated to preset temperature, the preset temperature that obtains is 45～95 ℃ water inlet 17 ' the enter membrane distillation assembly 6 that is immersed in the heating water tank 5, the side 8 that sees through of membrane distillation assembly 6 is passed through vacuum pump 12 via condenser 9, gas-liquid separator 10 and surge tank 11 vacuumize formation-0.01～-negative pressure of 0.1MPa, seeing through under side 8 vacuum action, preset temperature be 45～95 ℃ water inlet 17 ' in gas, the fenestra of steam permeable membrane distillation assembly 6 is seeing through side 8 formation water vapor and other gases 18, water vapor and other gas 18 are by condenser 9 condensations, and form membrane distillations through gas-liquid separator 10 and produce water 19 and enter and produce water pot 13, remove to use water spot then; The discharging regularly of the dense water 20 of membrane distillation focuses on.
Among Fig. 3, pH is that 6.5～8.5 water inlet 14 enters heating water tank 5 and is heated to preset temperature, the preset temperature that obtains is that 45～95 ℃ water inlet 17 " after liquid meter 2 metering by fresh feed pump 4 " enters membrane distillation assembly 6 from the hot side 7 of membrane distillation assembly 6, the side 8 that sees through of membrane distillation assembly 6 is passed through vacuum pump 12 via condenser 9, gas-liquid separator 10 and surge tank 11 vacuumize formation-0.01～-negative pressure of 0.1MPa, seeing through under side 8 vacuum action, the water inlet 17 that preset temperature is 45～95 ℃ " in gas; the fenestra of steam permeable membrane distillation assembly 6 forms water vapors and other gases 18 seeing through side 8; water vapor and other gases 18 are by condenser 9 condensations; and form membrane distillations through gas-liquid separator 10 and produce water 19 and enter and produce water pot 13, removes to use water spot then; The dense water 20 of membrane distillation leaves and can be used as into that the part of water is circulated back to heating water tank 5 or discharging regularly focuses on behind the membrane distillation assembly 6.
Embodiment
Embodiment 1:
The reverse osmosis concentrated water of certain petroleum chemical enterprise, main water quality characteristic is: sewage pH 8, electricity is led 25mS/cm, COD
Cr242mg/L, Ca
2+214mg/L, Mg
2+227mg/L, Na
+5078mg/L, Cl
-8407mg/L, molten silicon 36mg/L, NH
4-N 2mg/L, turbidity 2NTU.Process flow diagram is seen Fig. 1.
Used membrane distillation assembly is tetrafluoroethylene plate and frame hydrophobic membrane assembly, and membrane pore size is 0.2 μ m.
Flow process is as follows: at first, be that 0.08: 1 air forms the influent gas liquid mixture as dissolving in gas-liquid volume ratio by air dissolved pump in the reverse osmosis concentrated water of pH 8 of water inlet, water inlet is measured by liquid meter and gas meter respectively with the amount of air; The influent gas liquid mixture enters heating water tank under the air dissolved pump effect, be heated to enter the membrane distillation assembly that is immersed in the heating water tank behind 75 ℃ of the preset temperatures and carry out membrane distillation; By vacuum pump via condenser, gas-liquid separator and the surge tank negative pressure that side vacuumizes formation-0.1MPa that sees through to the membrane distillation assembly; Then, seeing through under the effect that side vacuumizes, the fenestra of the gas in the influent gas liquid mixture, steam permeable membrane distillation assembly by condenser condenses, and forms membrane distillation through gas-liquid separator and produces water and enter the product water pot, removes to use water spot then; The dense water of membrane distillation in the heating water tank regularly discharging centrally disposes.
Under this operational condition, the membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Embodiment 2:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Embodiment 3:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Embodiment 4:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Embodiment 5:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Comparative Examples 1:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 2.
Comparative Examples 1 membrane distillation process is as different from Example 1: as the reverse osmosis concentrated water of water inlet by the liquid meter metering after, directly enter heating water tank, be heated to and enter the membrane distillation assembly that is immersed in the heating water tank behind 75 ℃ of the preset temperatures and carry out membrane distillation; Other membrane distillation treatment condition are identical with embodiment 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
Comparative Examples 2:
The main water quality characteristic of the reverse osmosis concentrated water of certain petroleum chemical enterprise is with embodiment 1.Process flow diagram is seen Fig. 3.
Comparative Examples 2 used membrane distillation assemblies are polypropylene hollow fiber hydrophobic membrane assembly, and membrane pore size is 0.2 μ m.Its membrane distillation process is as different from Example 1: directly enter heating water tank as the reverse osmosis concentrated water of water inlet and be heated to 75 ℃ of preset temperatures, after the liquid meter metering, enter the membrane distillation assembly by fresh feed pump and carry out membrane distillation, the flow velocity of water inlet is 0.6m/s; To the negative pressure that side (in the hollow fiber film assembly fenestra) vacuumizes formation-0.1MPa that sees through of membrane distillation assembly, other membrane distillation treatment condition are identical with embodiment 1.
The membrane distillation treatment effect of reverse osmosis concentrated water sees Table 2.
The membrane distillation treatment effect of table 2 reverse osmosis concentrated water
Claims (10)
1. the molten gas vacuum membrane distillation of immersion water treatment method comprises:
Steps A, water inlet are mixed formation influent gas liquid mixture with gas;
Step B, the influent gas liquid mixture enters heating water tank, is heated to the influent gas liquid mixture that preset temperature obtains preset temperature;
Step C vacuumizes the formation negative pressure in the side that sees through of membrane distillation assembly;
Step D is seeing through under the side vacuum action, the fenestra of the gas in the influent gas liquid mixture of preset temperature, steam permeable membrane distillation assembly, and seeing through side condensation formation membrane distillation product water;
Wherein, steps A is dissolved in into water formation influent gas liquid mixture by air dissolved pump with gas.
2. method according to claim 1 is characterized in that: gas described in the steps A is nitrogen, oxygen or airborne a kind of or two kinds; The volume ratio of gas and liquid is 0.01: 1～0.5: 1 in the described influent gas liquid mixture.
3. method according to claim 2, it is characterized in that: the volume ratio of gas and liquid is 0.08: 1～0.2: 1 in the described influent gas liquid mixture.
4. method according to claim 1, it is characterized in that: the liquid mixture of influent gas described in the step B enters heating water tank by air dissolved pump.
5. method according to claim 1, it is characterized in that: the preset temperature of the described water inlet of step B is 45～95 ℃.
6. method according to claim 5, it is characterized in that: the preset temperature of described water inlet is 65～85 ℃.
7. method according to claim 1, it is characterized in that: the assembly of membrane distillation described in the step C is immersed in the heating water tank.
8. method according to claim 1, it is characterized in that: the assembly of membrane distillation described in the step C comprises tubular fibre curtain type film assembly or plate and frame module; The mould material of described membrane distillation assembly is polyvinylidene difluoride (PVDF), tetrafluoroethylene or microporous polypropylene membrane material; Wherein, the pore diameter range of described microporous membrane material is 0.1～0.5 μ m, and the pore diameter range of preferred described microporous membrane material is 0.15～0.22 μ m.
9. method according to claim 1 is characterized in that: the seeing through wall pressure and be-0.01 of the assembly of membrane distillation described in the step C～-0.1MPa.
10. method according to claim 9 is characterized in that: the seeing through wall pressure and be-0.085 of described membrane distillation assembly～-0.1MPa.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103803669A (en) * | 2013-12-26 | 2014-05-21 | 许昌学院 | Desalination device and desalination method for brackish water and seawater through air purging and vacuum membrane distillation |
| CN104415666A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | Immersed vacuum membrane distillation concentration method of ethylene glycol solution |
| CN111285431A (en) * | 2020-03-27 | 2020-06-16 | 中国华能集团清洁能源技术研究院有限公司 | Ultrasonic-assisted membrane distillation water treatment system and method |
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| CN101327407A (en) * | 2007-06-20 | 2008-12-24 | 天津工业大学 | Apparatus and method for evaporating and concentrating liquid |
| CN101664642A (en) * | 2008-09-04 | 2010-03-10 | 天津工业大学 | Device and method for air-blowing vacuum membrane distillation |
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- 2012-01-06 CN CN201210003547.8A patent/CN103193295B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101327407A (en) * | 2007-06-20 | 2008-12-24 | 天津工业大学 | Apparatus and method for evaporating and concentrating liquid |
| CN101664642A (en) * | 2008-09-04 | 2010-03-10 | 天津工业大学 | Device and method for air-blowing vacuum membrane distillation |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104415666A (en) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | Immersed vacuum membrane distillation concentration method of ethylene glycol solution |
| CN104415666B (en) * | 2013-08-20 | 2016-09-21 | 中国石油化工股份有限公司 | The immersion vacuum membrane distillation method for concentration of ethylene glycol solution |
| CN103803669A (en) * | 2013-12-26 | 2014-05-21 | 许昌学院 | Desalination device and desalination method for brackish water and seawater through air purging and vacuum membrane distillation |
| CN111285431A (en) * | 2020-03-27 | 2020-06-16 | 中国华能集团清洁能源技术研究院有限公司 | Ultrasonic-assisted membrane distillation water treatment system and method |
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