CN103357188A - Method and equipment for concentrating brackish water - Google Patents
Method and equipment for concentrating brackish water Download PDFInfo
- Publication number
- CN103357188A CN103357188A CN2012100799405A CN201210079940A CN103357188A CN 103357188 A CN103357188 A CN 103357188A CN 2012100799405 A CN2012100799405 A CN 2012100799405A CN 201210079940 A CN201210079940 A CN 201210079940A CN 103357188 A CN103357188 A CN 103357188A
- Authority
- CN
- China
- Prior art keywords
- air
- brackish water
- tower
- heater
- cold
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a method and equipment for concentrating brackish water. The method disclosed by the invention comprises the following steps that (1), after being heated by a brackish water pre-heater (14) and a brackish water heater (15), brackish water enters an evaporation chamber (2) of a hot concentration tower; (2), after being heated by a heater (1), air enters the evaporation chamber (2); mass transfer and heat transfer between brackish water and air are carried out in the evaporation chamber; (3), the mixture of air and steam discharged from the top of the evaporation chamber (2) enters the shell side of the cooler (7) to be cooled by heat conduction liquid; the heated heat conduction liquid is sent into the heater (1) and a cooling tower heater (9) to heat air and then sent into the brackish water pre-heater (14) to pre-heat brackish water; and (4), air heated by the cooling tower heater (9) enters an evaporation chamber (10) of a cooling tower and transfers mass and heat with brackish water from the bottom of the evaporation chamber (2); after salt is separated, brackish water concentrated for the second time returns to the system. The invention further relates to equipment for the method.
Description
Technical field
The present invention relates to brackish water concentration technique field, especially relates to a kind of utilization brackish water is carried out the method and apparatus that concentration and evaporation is processed.
Background technology
In at present common circulating water cooling tower, adopt the mode of empty G﹠W convection current transmission of heat by contact to allow a part of water enter in the air, reach water-cooled purpose, the present invention utilizes this principle, design a kind of method and apparatus that utilizes air that brackish water is concentrated, this equipment is made of hot concentration tower, cold concentration tower and salt making system; In hot concentration tower, utilize hot-air that the high temperature low concentration brackish water through heating is carried out concentrating at hot concentration tower the first time, utilize simultaneously the conductive fluid circulatory system to reclaim the heat of the concentrated over-the-top vapour (OTTV) of heat and air mixture, be used for heating brackish water and the air that enters hot concentration tower and cold concentration tower; It is concentrated that the low temperature and high concentration brackish water that the air that utilization is heated by conductive fluid comes hot concentration tower carries out second time at cold concentration tower, and the brackish water after concentrating for the second time enters analyses the salt pond, and the brackish water retrieval system of separating out behind the salinity concentrates again.
Method of the present invention and utilized air as the mass-and heat-transfer medium has effectively prevented equipment corrosion; Utilize heat recovery system to reach higher heat recovery and utilization effect, saved energy.
Summary of the invention
The present invention at first provides a kind of hot concentration tower, and a kind of cold concentration tower has following characteristics:
Hot concentration tower is comprised of parts such as shell, heater (1), vaporization chamber (2), air vent (3), water-locator (4), air-introduced machine (5), air channel (6), cooler (7) and various pipe joints; Hot concentration tower bottom is provided with air inlet, and air inlet top is heater (1), and heater (1) cover top portion links to each other with vaporization chamber (2) shell middle and lower part, the vaporization chamber bottom lock, and the above is provided with the brackish water outlet; Be provided with air vent (3) on the shell between heater (1) shell and vaporization chamber (2) shell junction and the vaporization chamber bottom, vaporization chamber (2) bottom is collecting-tank, the middle part is evaporating space, top arranges water-locator (4), water-locator (4) top is air-introduced machine (5), and air-introduced machine (5) top is air channel (6), and air channel (6) link to each other with cooler (7) shell, cooler (7) outer casing bottom is the demineralized water outlet, and the top is drain.
Cold concentration tower structure is similar with hot concentration tower, but does not have air channel, cooling chamber and cooler.Cold concentration tower bottom is air intake, the air intake top is cold tower heater (9), and cold tower heater (9) top is cold tower vaporization chamber (10), and cold tower vaporization chamber (10) top is water-locator, water-locator top is cold tower air-introduced machine (11), and cold tower air-introduced machine top is drain.
The outlet of the cooler of hot concentration tower (7) tube side links to each other with cold tower heater (9), brackish water preheater (14) the tube side entrance of the heater (1) of hot concentration tower, cold concentration tower; The cold tower heater (9) of the heater of hot concentration tower (1), cold concentration tower, the outlet of brackish water preheater (14) tube side link to each other with conductive fluid circulating pump (8) entrance; Conductive fluid circulating pump (8) outlet links to each other with cooler (7) the tube side entrance of hot concentration tower, consists of conductive fluid circulated heat recovery system.
Adopt above-mentioned hot concentration tower and cold concentration tower, can provide a kind of brackish water is carried out the method for concentration,
May further comprise the steps:
(1) brackish water sent here of the external world and mix from analysing the brackish water that returns in the salt pond, at first in brackish water preheater (14), be preheated, then enter brackish water heater (15) and be heated to higher temperature, the heat of brackish water preheater comes from from the next conductive fluid of cooler, and the heat of brackish water heater comes from extraneous next heat medium (such as conductive fluid, steam or flue gas).Brackish water after the heating enters hot concentration tower from hot concentration tower vaporization chamber (2) top through water-locator (4).
(2) air enters from hot concentration tower bottom, be heated by the heater shell side, heated air enters vaporization chamber from passage, and the next brackish water mass-and heat-transfer in evaporating column of step (1), part water is vaporized and enters the mixture that forms air and steam in the air, enters cold concentration tower after brackish water is concentrated.
(3) mixture of the air of step (2) and steam enters cooler (7) shell side by air channel (6) and is cooled, and conductive fluid is heated; Part water in air after being cooled and the mixture of steam is condensed out, discharges from the cooler casing bottom and reclaims, and the mixture of surplus air and steam is from cooler casing top drain row atmosphere; Heated conductive fluid is sent to heater (1) and cold tower heater (9) adds hot-air, is sent to brackish water preheater (14) preheating brackish water, and the conductive fluid that is cooled in heat exchanger (1,9,14) is returned cooler (7) by the heat conduction liquid pump.
(4) air enters cold tower heater shell side from cold concentration tower bottom and is heated, heated air enters cold tower vaporization chamber by passage, and the next brackish water mass-and heat-transfer in cold tower vaporization chamber of step (2), part water is vaporized and enters the mixture that forms air and steam in the air, and brackish water is concentrated; The mixture of air and steam is by cold tower blower fan (11) row atmosphere, and the brackish water that is concentrated enters analyses salt pond (12); Return hot concentration tower brackish water inlet line at the brackish water of analysing after salinity is separated out in the salt pond by brine pump (13).
Method of the present invention utilizes cold tower heater (9), brackish water preheater (14) and conductive fluid circulating pump (8) by the heater (1) of the cooler (7) of hot concentration tower, hot concentration tower, cold concentration tower to consist of conductive fluid circulated heat recovery system with the steam of hot concentration tower vaporization chamber discharge and the heat recovery of air mixture.
Method of the present invention, the heat that utilizes cold concentration tower that heat and the part of the brackish water of hot concentration tower discharge are come by conductive fluid circulated heat recovery system is further recycled.
The method and apparatus of brackish water concentration of the present invention has following characteristics and effect:
The first, the comprehensive utilization of energy:
Method of the present invention is compared with multiple-effect evaporation, utilizes conductive fluid circulated heat recovery system with the steam of hot concentration tower vaporization chamber discharge and the heat recovery of air mixture; The heat that utilizes cold concentration tower that heat and the part of the brackish water of hot concentration tower discharge are come by conductive fluid circulated heat recovery system is further recycled, and has saved energy.
The second, the comprehensive utilization of material:
The present invention has reclaimed partial deionization water when reclaiming heat.
Three, equipment protection:
Hot concentration tower and cold concentration tower all adopt the mode of direct contact type mass-and heat-transfer, do not need heat exchanger tube, have prevented obstruction and the corrosion of the normal equipment that occurs in the tubular type evaporation.In the heat-exchange system of the present invention except brackish water preheater and brackish water heater need special anticorrosion material other equipment be common material, compare with common multiple-effect evaporation and greatly reduce equipment investment, improved the equipment cycle of operation.
Description of drawings
Fig. 1 is the process equipment schematic diagram of the invention process example, wherein:
1: heater;
2: vaporization chamber;
3: air vent;
4: water-locator;
5: air-introduced machine;
6: the air channel;
7: cooler;
8: the conductive fluid circulating pump;
9: cold tower heater;
10: cold tower vaporization chamber;
11: cold tower blower fan;
12: analyse the salt pond;
13: brine pump;
14, brackish water preheater;
15: the brackish water heater.
The specific embodiment
As shown in Figure 1, method of the present invention, preferably undertaken by following technology and equipment:
The brackish water that the external world sends here and mix from analysing the brackish water that returns in the salt pond, at first in brackish water preheater (14), be preheated, then enter brackish water heater (15) and be heated to higher temperature, the heat of brackish water preheater comes from from the next conductive fluid of cooler, and the heat of brackish water heater comes from extraneous next heat medium (such as conductive fluid, steam or flue gas).Brackish water after the heating enters hot concentration tower from hot concentration tower vaporization chamber (2) top through water-locator (4).Air enters from hot concentration tower bottom, be heated by the heater shell side, heated air enters vaporization chamber and from brackish water mass-and heat-transfer evaporating column of brackish water heater (15) from air vent, part water is vaporized and enters the mixture that forms air and steam in the air, brackish water is concentrated, the brackish water that is concentrated enters cold concentration tower, and the mixture of steam enters cooler (7) shell side by air channel (6) and is cooled, and conductive fluid is heated; Part water in the mixture of the empty G﹠W after being cooled is condensed out, discharges from the cooler casing bottom and reclaims, and the mixture of surplus air and steam is from cooler casing top drain row atmosphere; Heated conductive fluid is sent to heater (1) and cold tower heater (9) adds hot-air, is sent to brackish water preheater (14) preheating brackish water, and the conductive fluid that is cooled in heat exchanger (1,9,14) is returned cooler (7) by the conductive fluid circulating pump.Air is heated from the shell side that cold concentration tower bottom enters cold tower heater (9), heated air enters cold tower vaporization chamber (10) from passage, brackish water in cold tower vaporization chamber the mass-and heat-transfer next with hot concentration tower vaporization chamber (2), part water is vaporized and enters the mixture that forms air and steam in the air, and brackish water is concentrated; The mixture of air and steam is by cold tower blower fan (11) row atmosphere, and the brackish water that is concentrated enters analyses salt pond (12); Return hot concentration tower brackish water inlet line at the brackish water of analysing after salinity is separated out in the salt pond by brine pump (13).
As shown in Figure 1, the used equipment concrete structure of method of the present invention is as follows:
Hot concentration tower: formed by parts such as shell, heater (1), vaporization chamber (2), air vent (3), water-locator (4), air-introduced machine (5), air channel (6), cooler (7) and various pipe joints; Hot concentration tower bottom is provided with air inlet, air inlet top is heater (1), heater (1) cover top portion links to each other with vaporization chamber (2) shell middle and lower part, the vaporization chamber bottom lock, the above is provided with the brackish water outlet, be provided with air vent (3) on the shell between heater (1) shell and vaporization chamber (2) shell junction and the vaporization chamber bottom, vaporization chamber (2) bottom is collecting-tank, the middle part is evaporating space, top arranges water-locator (4), water-locator (4) top is air-introduced machine (5), air-introduced machine (5) top is air channel (6), air channel (6) links to each other with cooler (7) shell, and cooler (7) outer casing bottom is the demineralized water outlet, and the top is drain.
Cold concentration tower: structure is similar with hot concentration tower, but does not have air channel, cooling chamber and cooler.Cold concentration tower bottom is air intake, the air intake top is cold tower heater (9), and cold tower heater (9) top is cold tower vaporization chamber (10), and cold tower vaporization chamber (10) top is water-locator, water-locator top is cold tower air-introduced machine (11), and cold tower air-introduced machine top is drain.
Conductive fluid circulated heat recovery system: the outlet of the cooler of hot concentration tower (7) tube side links to each other with cold tower heater (9), brackish water preheater (14) the tube side entrance of the heater (1) of hot concentration tower, cold concentration tower; The cold tower heater (9) of the heater of hot concentration tower (1), cold concentration tower, the outlet of brackish water preheater (14) tube side link to each other with conductive fluid circulating pump (8) entrance; Conductive fluid circulating pump (8) outlet links to each other with cooler (7) the tube side entrance of hot concentration tower, consists of conductive fluid circulated heat recovery system.
Method of the present invention, brackish water preheater, brackish water heater can adopt lamella heat exchanger or lamella heat exchanger as required, and cooler, thermal tower heater, cold tower heater can adopt finned tube exchanger or lamella heat exchanger as required.
Above-described embodiment is described preferred embodiment of the present invention; be not that scope of the present invention is limited; design under the prerequisite of spirit not breaking away from the present invention; various distortion and improvement that the common engineers and technicians in this area make technical scheme of the present invention all should fall in the definite protection domain of claims of the present invention.
Claims (7)
1. the invention provides a kind of hot concentration tower, have following characteristics:
Hot concentration tower is comprised of parts such as shell, heater (1), vaporization chamber (2), air vent (3), water-locator (4), air-introduced machine (5), air channel (6), cooler (7) and various pipe joints; Hot concentration tower bottom is provided with air inlet, and air inlet top is heater (1), and heater (1) cover top portion links to each other with vaporization chamber (2) shell middle and lower part, the vaporization chamber bottom lock, and the above is provided with the brackish water outlet; Be provided with air vent (3) on the shell between heater (1) shell and vaporization chamber (2) shell junction and the vaporization chamber bottom, vaporization chamber (2) bottom is collecting-tank, the middle part is evaporating space, top arranges water-locator (4), water-locator (4) top is air-introduced machine (5), and air-introduced machine (5) top is air channel (6), and air channel (6) link to each other with cooler (7) shell, cooler (7) outer casing bottom is the demineralized water outlet, and the top is drain.
2. the invention provides a kind of cold concentration tower, have following characteristics:
Cold concentration tower structure is similar with hot concentration tower, but does not have air channel, cooling chamber and cooler; Cold concentration tower bottom is air intake, the air intake top is cold tower heater (9), and cold tower heater (9) top is cold tower vaporization chamber (10), and cold tower vaporization chamber (10) top is water-locator, water-locator top is cold tower air-introduced machine (11), and cold tower air-introduced machine top is drain.
3. a kind of conductive fluid circulated heat recovery system provided by the invention has following characteristics:
The outlet of the cooler of hot concentration tower (7) tube side links to each other with cold tower heater (9), brackish water preheater (14) the tube side entrance of the heater (1) of hot concentration tower, cold concentration tower; The cold tower heater (9) of the heater of hot concentration tower (1), cold concentration tower, the outlet of brackish water preheater (14) tube side link to each other with conductive fluid circulating pump (8) entrance; Conductive fluid circulating pump (8) outlet links to each other with cooler (7) the tube side entrance of hot concentration tower, consists of conductive fluid circulated heat recovery system.
4. adopt above-mentioned hot concentration tower and cold concentration tower, can provide a kind of brackish water is carried out the method for concentration, may further comprise the steps:
(1) brackish water sent here of the external world and mix from analysing the brackish water that returns in the salt pond, at first in brackish water preheater (14), be preheated, then enter brackish water heater (15) and be heated to higher temperature, the heat of brackish water preheater comes from from the next conductive fluid of cooler, the heat of brackish water heater comes from extraneous next heat medium (such as conductive fluid, steam or flue gas), and the brackish water after the heating enters hot concentration tower from hot concentration tower vaporization chamber (2) top through water-locator (4); Air enters from hot concentration tower bottom, be heated by the heater shell side, heated air enters vaporization chamber from passage, with heated brackish water mass-and heat-transfer in evaporating column, part water is vaporized and enters the mixture that forms air and steam in the air, enters cold concentration tower after brackish water is concentrated; The mixture of air and steam enters cooler (7) shell side by air channel (6) and is cooled, and conductive fluid is heated; Part water in air after being cooled and the mixture of steam is condensed out, discharges from the cooler casing bottom and reclaims, and the mixture of surplus air and steam is from cooler casing top drain row atmosphere; Heated conductive fluid is sent to heater (1) and cold tower heater (9) adds hot-air, is sent to brackish water preheater (14) preheating brackish water, and the conductive fluid that is cooled in heat exchanger (1,9,14) is returned cooler (7) by the heat conduction liquid pump.
5.(2) air enters cold tower heater shell side from cold concentration tower bottom and be heated, heated air enters cold tower vaporization chamber by passage, and the next brackish water mass-and heat-transfer in cold tower vaporization chamber of step (2), part water is vaporized and enters the mixture that forms air and steam in the air, and brackish water is concentrated; The mixture of air and steam is by cold tower blower fan (11) row atmosphere, and the brackish water that is concentrated enters analyses salt pond (12); Return hot concentration tower brackish water inlet line at the brackish water of analysing after salinity is separated out in the salt pond by brine pump (13).
6. method of the present invention utilizes cold concentration tower that heat and the part of the brackish water of hot concentration tower discharge are further recycled by the next heat of conductive fluid circulated heat recovery system.
7. method of the present invention, brackish water preheater, brackish water heater can adopt lamella heat exchanger or lamella heat exchanger as required, and cooler, thermal tower heater, cold tower heater can adopt finned tube exchanger or lamella heat exchanger as required.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100799405A CN103357188A (en) | 2012-03-26 | 2012-03-26 | Method and equipment for concentrating brackish water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100799405A CN103357188A (en) | 2012-03-26 | 2012-03-26 | Method and equipment for concentrating brackish water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103357188A true CN103357188A (en) | 2013-10-23 |
Family
ID=49359961
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012100799405A Pending CN103357188A (en) | 2012-03-26 | 2012-03-26 | Method and equipment for concentrating brackish water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103357188A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106823422A (en) * | 2017-04-10 | 2017-06-13 | 徐燚 | Solution condensing device |
| CN108905241A (en) * | 2018-06-29 | 2018-11-30 | 江苏海容热能环境工程有限公司 | A kind of brine concentration and concentration regulator |
| CN109534583A (en) * | 2019-01-11 | 2019-03-29 | 中工沃特尔水技术股份有限公司 | High-salt wastewater concentration systems and method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4310382A (en) * | 1979-01-25 | 1982-01-12 | Schering Ag | Method of and a device for vaporizing and recovering water from aqueous solutions |
| JP2004121995A (en) * | 2002-10-02 | 2004-04-22 | Ebara Corp | Vacuum evaporation type distillation equipment |
| JP2005313117A (en) * | 2004-04-30 | 2005-11-10 | Toshihiro Abe | Method and apparatus for evaporation concentration |
| CN1864783A (en) * | 2006-04-30 | 2006-11-22 | 周堃 | A multi-effect distilling method for desalt and condensation and device |
| JP2008272668A (en) * | 2007-04-27 | 2008-11-13 | Saline Water Conversion Corp | Water producing apparatus and water producing method |
| CN102603023A (en) * | 2012-03-23 | 2012-07-25 | 郭朝军 | Method and equipment for carrying out evaporation-concentration treatment on saline water by utilizing solar energy and air |
| CN202909470U (en) * | 2012-03-24 | 2013-05-01 | 郭朝军 | Evaporation tower for performing evaporation treatment on salt-containing water using gas |
-
2012
- 2012-03-26 CN CN2012100799405A patent/CN103357188A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4310382A (en) * | 1979-01-25 | 1982-01-12 | Schering Ag | Method of and a device for vaporizing and recovering water from aqueous solutions |
| JP2004121995A (en) * | 2002-10-02 | 2004-04-22 | Ebara Corp | Vacuum evaporation type distillation equipment |
| JP2005313117A (en) * | 2004-04-30 | 2005-11-10 | Toshihiro Abe | Method and apparatus for evaporation concentration |
| CN1864783A (en) * | 2006-04-30 | 2006-11-22 | 周堃 | A multi-effect distilling method for desalt and condensation and device |
| JP2008272668A (en) * | 2007-04-27 | 2008-11-13 | Saline Water Conversion Corp | Water producing apparatus and water producing method |
| CN102603023A (en) * | 2012-03-23 | 2012-07-25 | 郭朝军 | Method and equipment for carrying out evaporation-concentration treatment on saline water by utilizing solar energy and air |
| CN202909470U (en) * | 2012-03-24 | 2013-05-01 | 郭朝军 | Evaporation tower for performing evaporation treatment on salt-containing water using gas |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106823422A (en) * | 2017-04-10 | 2017-06-13 | 徐燚 | Solution condensing device |
| CN108905241A (en) * | 2018-06-29 | 2018-11-30 | 江苏海容热能环境工程有限公司 | A kind of brine concentration and concentration regulator |
| CN109534583A (en) * | 2019-01-11 | 2019-03-29 | 中工沃特尔水技术股份有限公司 | High-salt wastewater concentration systems and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202860146U (en) | Combined equipment for concentrating salt-containing water | |
| CN102603023B (en) | Method and equipment for carrying out evaporation-concentration treatment on saline water by utilizing solar energy and air | |
| CN207761721U (en) | Coke oven ascension pipe crude gas ORC power generation system | |
| CN105883736A (en) | Efficient and low-pollution phosphorous-slurry recycling method | |
| CN107940426A (en) | Overcritical pyrolyzing coal pneumoelectric sprays flash boiler | |
| CN102925165A (en) | Afterheat recovery system for raw coke oven gas of coke oven ascension pipe | |
| CN104645649A (en) | Liquid distillation equipment | |
| CN105363227A (en) | Mechanical vapor recompression system and mechanical vapor recompression method based on same | |
| CN107144146A (en) | Can-type calcine furnace afterheat utilizing system based on piping-main scheme | |
| CN103357188A (en) | Method and equipment for concentrating brackish water | |
| CN104313267A (en) | Device for realizing salt and water recycling by utilizing salt quenching waste heat | |
| CN204100844U (en) | Thermal power plant's Air-cooled Unit hot-air recycling system | |
| CN102058994B (en) | Device and method for condensing, drying and heating flue gas | |
| CN204656030U (en) | A kind of liquid distillation equipment | |
| CN106623215A (en) | Energy-saving recycling method of hydrocarbon cleaning agent and hydrocarbon cleaning equipment | |
| CN205782821U (en) | High steam recovery system | |
| CN100534896C (en) | Method of utilizing waste heat after boiling furnace in sulfuric acid production | |
| CN104645646A (en) | Total heat and latent heat recovery type multi-effect vacuum evaporation and concentration device | |
| CN105366864B (en) | Oil drilling waste processing system and its method for handling oil drilling waste | |
| CN103968666B (en) | A kind of smelting furnace of aluminum or aluminum alloy production | |
| CN214512794U (en) | Non-condensable gas recovery system of evaporation system | |
| CN206369491U (en) | A kind of printing and dyeing enterprise flue gas waste heat recovery system based on heat pipe | |
| RU2555919C1 (en) | Surface-mounted heat recovery unit for deep heat recovery of flue gases, and its operation method | |
| CN202881181U (en) | Crude gas waste heat recovery system used for coke oven ascension pipe | |
| CN109825705B (en) | Device and method for recycling mercury from waste mercury catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C05 | Deemed withdrawal (patent law before 1993) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20131023 |