CN102658030A - Liquid and membrane non-contact barrel-shaped membrane distiller - Google Patents
Liquid and membrane non-contact barrel-shaped membrane distiller Download PDFInfo
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- CN102658030A CN102658030A CN2012101475901A CN201210147590A CN102658030A CN 102658030 A CN102658030 A CN 102658030A CN 2012101475901 A CN2012101475901 A CN 2012101475901A CN 201210147590 A CN201210147590 A CN 201210147590A CN 102658030 A CN102658030 A CN 102658030A
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- 239000007788 liquid Substances 0.000 title claims abstract description 64
- 239000012528 membrane Substances 0.000 title abstract description 36
- 239000012530 fluid Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 230000002209 hydrophobic effect Effects 0.000 claims abstract description 18
- 238000009833 condensation Methods 0.000 claims abstract description 17
- 230000005494 condensation Effects 0.000 claims abstract description 17
- 239000004744 fabric Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 18
- 230000008676 import Effects 0.000 claims description 15
- 238000005276 aerator Methods 0.000 claims description 10
- 239000002912 waste gas Substances 0.000 claims description 10
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 9
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 9
- 239000002826 coolant Substances 0.000 claims description 7
- 239000012153 distilled water Substances 0.000 claims description 4
- 230000004888 barrier function Effects 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 238000004821 distillation Methods 0.000 abstract description 27
- 238000012546 transfer Methods 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000005273 aeration Methods 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000007246 mechanism Effects 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 238000001816 cooling Methods 0.000 abstract description 3
- 239000012982 microporous membrane Substances 0.000 abstract description 2
- 239000013535 sea water Substances 0.000 abstract description 2
- 238000010408 sweeping Methods 0.000 abstract description 2
- 239000008399 tap water Substances 0.000 abstract 1
- 235000020679 tap water Nutrition 0.000 abstract 1
- 238000000034 method Methods 0.000 description 21
- 230000008569 process Effects 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000010287 polarization Effects 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 238000009736 wetting Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003064 anti-oxidating effect Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
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- 238000011160 research Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a liquid and membrane non-contact barrel-shaped membrane distiller. The distiller comprises a water vapor generation system, a gas generation system, a condensation and liquid collection system and a membrane barrel, wherein the membrane barrel comprises a liquid distribution aeration chamber and a permeable membrane gas collection chamber; the permeable membrane gas collection chamber is formed above the liquid distribution aeration chamber; and an internal contact membrane is arranged in the permeable membrane gas collection chamber. The mass transfer mechanism of the liquid and membrane non-contact barrel-shaped membrane distiller is that mass transfer is directly performed by using the pressure difference of gas instead of the difference of partial pressure of water vapor, so mass transfer efficiency is high; compared with sweeping gas membrane distillation, non-contact membrane distillation has the advantages that compressed air is filtered and cleaned by a hydrophobic microporous membrane, so that the quality of produced water is high; the air is fully wetted, and gas consumption is low; compared with direct contact membrane distillation, the non-contact membrane distillation has the advantages that cold fluid and hot fluid are not directly contacted and condensed on the two sides of the membrane, so that energy consumption can be obviously reduced; compared with vacuum membrane distillation, the non-contact membrane distillation has the advantages that the energy consumption of an air compressor is lower than that of a vacuum pump, so that the utilization efficiency of electric energy is high; and the equipment requirement is simple, and liquid to be treated can be tap water, sea water, or hot water or a chemical product solution discharged by a cooling system.
Description
Technical field
The present invention relates to water treatment facilities, particularly a kind of liquid and not touch of film tubular film distiller.
Background technology
The film distillation is a kind of employing dewatering microporous film, is the film separation process of mass transfer driving force with film both sides steam pressure difference.Under the driving of the steam pressure difference of microporous hydrophobic membrane both sides, water vapour is condensed into liquid separation process again after heated former water one side is passed hydrophobic membrane.Because the hydrophobicity of film; Have only water vapour can see through fenestra; Former water and the non-volatile solute that is dissolved in wherein can't pass fenestra, so the film still-process in theory can removing ion, big molecule, colloid, cell and other non-volatile matter realization 100%.Microporous hydrophobic membrane plays the support shielding action between two phases in the film still-process.In the process of film distillation, two kinds of processes of heat and mass transfer take place simultaneously, temperature difference polarization also can produce with temperature difference polarization phenomena simultaneously, thereby the process of film distillation is produced adverse influence.The operating temperature of film still-process is lower than traditional still-process, and operating pressure is lower than traditional film separation process; Mechanical performance to film requires lower; Compare with traditional still-process, the vapor space significantly reduces.The assembly of film distillation can be designed to latent heat and reclaim form, and has with the flexibility of small-sized membrane module formation large-scale production system efficiently.This process can the high fortified aqueous of concentration of treatment; If solute is the material of easy and crystalline; Can realize film distillation crystallization to solution concentration to hypersaturated state, be present unique can be from solution direct separation go out the membrane process of crystallized product, and as long as the suitable temperature difference is kept in the film both sides; This process just can be carried out, and can utilize solar energy, underground heat, hot spring, waste heat of plant and the warm cheap energy such as industrial wastewater.It is low that film distillation technology has an operating pressure, and salt rejection rate that can obtain 99. 99 % and the water flux that under the excellent operation condition, is higher than counter-infiltration are arranged, and shown its substituting (extensive pure water preparation) or replenishing technology as reverse osmosis technology.
On a large amount of film distillation researchs and experiment basis, present the development four kinds of different film distillation procedure modes for many years, comprises the distillation of direct contact type film, the distillation of GAP TYPE film, the distillation of gas flow purging formula film and the distillation of vacuum type film.Wherein contact method is the steam that sees through perforated membrane directly to be got into pure water at cold side carry out condensation, so condensation process is integrated in the membrane module, operate simply relatively, therefore is to be studied maximum a kind of films to distill mode.Yet compare with other mode of operation; Directly the contact membranes distillation can cause more heat loss and comparatively serious temperature difference polarization; Vacuum type film distillation rule is to apply a negative pressure through side, will be retracted to through the water vapour of perforated membrane in the condenser beyond the membrane module and carry out condensation liquefaction.The advantage of this process is that thermal loss is all littler than other three kinds of film distillation procedure methods, and distillating ventilating amount is higher, can cause the fenestra humidifying but the negative pressure that applies is lower than the pressure of liquid entering fenestra, and etc. shortcoming, heat and mass transfer mechanism also needs further to inquire into.At present existing above four kinds of films distillation mode all exists solution necessarily to have a side directly to contact porous hydrophobic membrane, is easy to generate hydrophobic membrane hydrophiling leakage problems, the blocking microporous film of solute substance fouling, some problems such as energy consumption is high simultaneously, efficient is low, reliability is low.Therefore, study new film distillation technology, reduce investment and operating cost, reduce the concentrated water discharge aspect, be expected to obtain remarkable economic efficiency and social benefit.
Summary of the invention
For solving the problems of the technologies described above; The invention provides a kind of liquid and not touch of film tubular film distiller, it has comprised aqueous vapor generation systems, gas generating system, condensation liquor collecting system and film tube, wherein; Said film tube has comprised cloth liquid solarization air cell; Pass through the film collection chamber, pass through the film collection chamber and be arranged on cloth liquid solarization air cell top, contact film in the film collection chamber is provided with thoroughly.
Preferably, said aqueous vapor generation systems has comprised fluid reservoir, woven hose and liquid back pipe, and woven hose is connected fluid reservoir and cloth liquid solarization air cell respectively with liquid back pipe.Preferably, the hydrothermal solution that provides of said aqueous vapor generation systems is not less than 70 degree.
Preferably, below cloth liquid solarization air cell, be provided with the hydrothermal solution import, woven hose connects this hydrothermal solution import, and the hot water in the fluid reservoir flows into cloth liquid solarization air cell via this hydrothermal solution import; Above cloth liquid solarization air cell, be provided with the hydrothermal solution outlet, liquid back pipe connects this hydrothermal solution outlet, and the hot water of cloth liquid solarization air cell flows back to fluid reservoir via said hydrothermal solution outlet;
Preferably, said gas generating system has comprised gas generator and appendix, and appendix connects gas generator and cloth liquid solarization air cell.
Preferably, in said cloth liquid solarization air cell, be provided with the microporous hydrophobic menbrane aerator, said appendix connects said microporous hydrophobic menbrane aerator.Preferred, said microporous hydrophobic menbrane aerator comprises the filter core that the folding microporous barrier of hydrophobicity PTFE is processed.
Preferably; Said condensation liquor collecting system: comprise aqueous vapor import, condenser, waste gas outlet, coolant outlet; The aqueous vapor that said film collection chamber comes out; Get into condenser through the aqueous vapor import, the distilled water of process condensation flows out from coolant outlet, and produced simultaneously waste gas is discharged from waste gas outlet.
Preferably, said condensation liquor collecting system also comprises the aqueous vapor refluxing opening, and the aqueous vapor that is not condensed is back to fluid reservoir.
Preferably, be provided with the fluid reservoir leakage fluid dram, be provided with solarization air cell's leakage fluid dram in said cloth liquid solarization air cell lower end in said fluid reservoir bottom.
Preferably, said interior contact film is a micropore PTFE film silk.
Liquid of the present invention and not touch of film tubular film distiller: its mechanism of mass transfer no longer is to utilize steam partial pressure poor, but direct gas differential pressure mass transfer, so mass-transfer efficiency is high; Sweeping the distillation of formula film with gas compares; Compressed air process hydrophobic microporous membrane filtration, cleaning, product water water quality is good; Air is wetting fully, and air consumption is few.Compare with the distillation of direct contact type film, cold fluid and hot fluid is directly cold undoubtful in the film contact both sides, can significantly cut down the consumption of energy.Compare with vacuum membrane distillation, the air compressor energy consumption is lower than vavuum pump, and utilization of power efficient is high; Equipment requirements is simple, and pending liquid can be the hot water or the chemical products solution of running water, seawater, cooling system discharge.
Description of drawings
Shown in Figure 1 for the structural representation of not touch of film tubular film distiller of the present invention;
Shown in Figure 2 for the structural representation of film tube of the present invention.
The specific embodiment
For make above-mentioned purpose of the present invention, feature and advantage can be more obviously understandable, does detailed explanation below in conjunction with the accompanying drawing specific embodiments of the invention, it will be more clear making above-mentioned and other purpose, characteristic and advantage of the present invention.Reference numeral identical in whole accompanying drawings is indicated identical part.Painstakingly do not draw accompanying drawing in proportion, focus on illustrating purport of the present invention.
Be illustrated in figure 1 as liquid of the present invention and not touch of film tubular film distiller structural representation; As shown in the figure, it has comprised aqueous vapor generation systems, gas generating system, condensation liquor collecting system and film tube, wherein; Said film tube has comprised cloth liquid solarization air cell 4; Pass through film collection chamber 8, pass through film collection chamber 8 and be arranged on cloth liquid solarization air cell 4 tops, contact film in film collection chamber 8 is provided with thoroughly.
The aqueous vapor generation systems has comprised fluid reservoir 11, woven hose 12 and liquid back pipe 13, and woven hose 12 is connected fluid reservoir 11 and cloth liquid solarization air cell 4 respectively with liquid back pipe 13.
Below cloth liquid solarization air cell 4, be provided with hydrothermal solution import 2, woven hose 12 connects this hydrothermal solution import 2, and 11 hot water flows into cloth liquid solarization air cell 4 via this hydrothermal solution import 2 in the fluid reservoir; Above cloth liquid solarization air cell, be provided with hydrothermal solution outlet 6, liquid back pipe 13 connects this hydrothermal solution outlet 6, and the hot water of cloth liquid solarization air cell flows back to fluid reservoir 11 via hydrothermal solution outlet 6; The hydrothermal solution that aqueous vapor provides is not less than 70 degree, through the circulation heating, guarantees that hot solution is not less than 70 degree.
The condensation liquor collecting system has comprised aqueous vapor import 14, condenser 15, waste gas outlet 16, coolant outlet 17.Pass through the aqueous vapor that film collection chamber 8 comes out, get into condenser 15 through aqueous vapor import 14, the distilled water of process condensation flows out from coolant outlet 17, and produced simultaneously waste gas is discharged from waste gas outlet 16.
The condensation liquor collecting system also comprises aqueous vapor refluxing opening 18, and the aqueous vapor that is not condensed is back to fluid reservoir.
Gas generating system has comprised gas generator 7 and appendix 9, and appendix 9 connects gas generator 7 and cloth liquid solarization air cell 4.In cloth liquid solarization air cell 4, be provided with microporous hydrophobic menbrane aerator 3, appendix 9 connects microporous hydrophobic menbrane aerator 3.The microporous hydrophobic menbrane aerator comprises the filter core that the folding microporous barrier of hydrophobicity PTFE is processed, and is external touch, and no shell directly is immersed in the former water, and compressed air is got in the former water with the micro-pore aeration mode by the inner film that sees through of hydrophobicity PTFE folded membrane filter core.Mainly be the density that improves aeration, filter the airborne pollutant of compression, hydrophobicity PTFE folded membrane aeration filter core is corrosion-resistant, acid and alkali-resistance, strong anti-oxidation.
Preferably, among the present invention, be provided with fluid reservoir leakage fluid dram 1, be used to regularly replace hydrothermal solution usefulness in fluid reservoir 11 bottoms, same, be provided with solarization air cell's leakage fluid dram 19 in cloth liquid solarization air cell lower end.
Preferably, contact film is a micropore PTFE film silk in this.
Among the present invention; Gas generating system with compressed air from gas generator 7 through microporous hydrophobic menbrane aerator 3; Bring the steam that the aqueous vapor generation systems produces into film collection chamber 8; See through the interior contact film (can constitute) that is fixed on the membrane module top, after the compressed air that former water is fully wetting sees through the micropore PTFE film silk internal membrane filtration of upper end, damp-heat air is incorporated into the condensation liquor collecting system from passing through the film collection chamber by the parallel connection of many film silk assemblies; The distilled water (product water) of this condenser system cooling is discharged through coolant outlet 17, and waste gas outlet 12 is used for combustion gas.
Because hot solution does not contact face; Can not produce hydrophobic membrane hydrophiling seepage, solute substance fouling blockage problem, mechanism of mass transfer no longer is to utilize steam partial pressure poor, but direct gas differential pressure mass transfer; Therefore mass-transfer efficiency is high, and energy consumption is low simultaneously, efficient is high, reliability is strong.Can utilize solar energy, underground heat, hot spring, waste heat of plant and the warm cheap energy such as industrial wastewater, realize that the film distillation of energy-conserving and environment-protective is used.
In above description, a lot of details have been set forth so that make much of the present invention.But above description only is preferred embodiment of the present invention, and the present invention can implement much to be different from alternate manner described here, so the present invention does not receive the restriction of top disclosed practical implementation.Any skilled personnel are not breaking away under the technical scheme scope situation of the present invention simultaneously; All the method for above-mentioned announcement capable of using and technology contents are made many possible changes and modification to technical scheme of the present invention, or are revised as the equivalent embodiment of equivalent variations.Every content that does not break away from technical scheme of the present invention to any simple modification, equivalent variations and modification that above embodiment did, all still belongs to technology of the present invention according to technical spirit of the present invention.
Claims (10)
1. liquid and not touch of film tubular film distiller; It has comprised aqueous vapor generation systems, gas generating system, condensation liquor collecting system and film tube; It is characterized in that said film tube has comprised cloth liquid solarization air cell, pass through the film collection chamber; Pass through the film collection chamber and be arranged on cloth liquid solarization air cell top, contact film in the film collection chamber is provided with thoroughly.
2. liquid as claimed in claim 1 and not touch of film tubular film distiller; It is characterized in that; Said aqueous vapor generation systems has comprised fluid reservoir, woven hose and liquid back pipe; Woven hose is connected fluid reservoir and cloth liquid solarization air cell respectively with liquid back pipe, and the hydrothermal solution that said aqueous vapor generation systems provides is not less than 70 degree.
3. liquid as claimed in claim 2 and not touch of film tubular film distiller is characterized in that, below cloth liquid solarization air cell, are provided with the hydrothermal solution import, and woven hose connects this hydrothermal solution import, and the hot water in the fluid reservoir flows into cloth liquid solarization air cell via this hydrothermal solution import; Above cloth liquid solarization air cell, be provided with the hydrothermal solution outlet, liquid back pipe connects this hydrothermal solution outlet, and the hot water of cloth liquid solarization air cell flows back to fluid reservoir via said hydrothermal solution outlet.
4. liquid as claimed in claim 1 and not touch of film tubular film distiller is characterized in that said gas generating system has comprised gas generator and appendix, and appendix connects gas generator and cloth liquid solarization air cell.
5. liquid as claimed in claim 4 and not touch of film tubular film distiller is characterized in that, in said cloth liquid solarization air cell, are provided with the microporous hydrophobic menbrane aerator, and said appendix connects said microporous hydrophobic menbrane aerator.
6. liquid as claimed in claim 5 and not touch of film tubular film distiller is characterized in that, said microporous hydrophobic menbrane aerator comprises the filter core that the folding microporous barrier of hydrophobicity PTFE is processed.
7. liquid as claimed in claim 1 and not touch of film tubular film distiller; It is characterized in that; Said condensation liquor collecting system: comprise aqueous vapor import, condenser, waste gas outlet, coolant outlet, the aqueous vapor that said film collection chamber comes out gets into condenser through the aqueous vapor import; Distilled water through condensation flows out from coolant outlet, and produced simultaneously waste gas is discharged from waste gas outlet.
8. liquid as claimed in claim 7 and not touch of film tubular film distiller is characterized in that said condensation liquor collecting system also comprises the aqueous vapor refluxing opening, and the aqueous vapor that is not condensed is back to fluid reservoir.
9. liquid as claimed in claim 7 and not touch of film tubular film distiller is characterized in that, are provided with the fluid reservoir leakage fluid dram in said fluid reservoir bottom, are provided with solarization air cell's leakage fluid dram in said cloth liquid solarization air cell lower end.
10. liquid as claimed in claim 1 and not touch of film tubular film distiller is characterized in that, said interior contact film is a micropore PTFE film silk.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101475901A CN102658030A (en) | 2012-05-14 | 2012-05-14 | Liquid and membrane non-contact barrel-shaped membrane distiller |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101475901A CN102658030A (en) | 2012-05-14 | 2012-05-14 | Liquid and membrane non-contact barrel-shaped membrane distiller |
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| CN102658030A true CN102658030A (en) | 2012-09-12 |
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| CN2012101475901A Pending CN102658030A (en) | 2012-05-14 | 2012-05-14 | Liquid and membrane non-contact barrel-shaped membrane distiller |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103212296A (en) * | 2013-04-18 | 2013-07-24 | 江苏夏航环境工程有限公司 | Gas-disturbance type membrane distilling method and membrane distilling device |
| CN114075503A (en) * | 2020-12-11 | 2022-02-22 | 北京百漾科技股份有限公司 | Method and equipment for distilling liqueur and liqueur |
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| CN1162929A (en) * | 1994-09-09 | 1997-10-22 | 泰斯特美克公司 | Method and system for extracting a solute from a fluid using dense gas and a porous membrane |
| CN101564649A (en) * | 2008-04-23 | 2009-10-28 | 天津工业大学 | Air compressing membrane distillation device and method |
| CN202638284U (en) * | 2012-05-14 | 2013-01-02 | 刘宁生 | Tubular membrane distillator capable of enabling liquid not to contact with membrane |
-
2012
- 2012-05-14 CN CN2012101475901A patent/CN102658030A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1162929A (en) * | 1994-09-09 | 1997-10-22 | 泰斯特美克公司 | Method and system for extracting a solute from a fluid using dense gas and a porous membrane |
| CN101564649A (en) * | 2008-04-23 | 2009-10-28 | 天津工业大学 | Air compressing membrane distillation device and method |
| CN202638284U (en) * | 2012-05-14 | 2013-01-02 | 刘宁生 | Tubular membrane distillator capable of enabling liquid not to contact with membrane |
Non-Patent Citations (2)
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| 姚汝华等: "《微生物工程工艺原理（第二版）》", 28 February 2007 * |
| 邹东恢: "《生物加工设备选型与应用》", 31 March 2009 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103212296A (en) * | 2013-04-18 | 2013-07-24 | 江苏夏航环境工程有限公司 | Gas-disturbance type membrane distilling method and membrane distilling device |
| CN103212296B (en) * | 2013-04-18 | 2015-03-11 | 江苏夏航环境工程有限公司 | Gas-disturbance type membrane distilling method and membrane distilling device |
| CN114075503A (en) * | 2020-12-11 | 2022-02-22 | 北京百漾科技股份有限公司 | Method and equipment for distilling liqueur and liqueur |
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Owner name: SHANGHAI FENGDU WATER PURIFICATION ENGINEERING CO. Free format text: FORMER OWNER: LIU NINGSHENG Effective date: 20121225 |
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Effective date of registration: 20121225 Address after: 200000 Shanghai City, Baoshan District Chemical Road No. 251 building 2001-2018 room two Applicant after: Shanghai Fengdu Water Purification Engineering Co., Ltd. Address before: Cang Xiang, Baixia District Nanjing 210000 Jiangsu province No. 9 Applicant before: Liu Ningsheng |
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Application publication date: 20120912 |