CN202808717U - Gasoline light fraction mercaptan removal and alkali liquid regeneration device - Google Patents
Gasoline light fraction mercaptan removal and alkali liquid regeneration device Download PDFInfo
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- CN202808717U CN202808717U CN 201220385221 CN201220385221U CN202808717U CN 202808717 U CN202808717 U CN 202808717U CN 201220385221 CN201220385221 CN 201220385221 CN 201220385221 U CN201220385221 U CN 201220385221U CN 202808717 U CN202808717 U CN 202808717U
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Abstract
The utility model relates to a gasoline light fraction mercaptan removal and alkali liquid regeneration device which comprises a static mixer, a liquid film alkali cleaning reactor, an alkali liquid coalescence removal device, an alkali liquid oxidation separation tower and a liquid film extraction contactor. According to the utility model, low investment is required for removing hydrogen sulfide and phenol by use of pre-alkali cleaning; by adopting a two-level liquid film alkali cleaning reactor and an alkali cleaning technology, mercaptan of the product can be guaranteed below 10ppm, entrainment of free alkali liquid is avoided, and the copper corrosion and water-soluble acid-base detection can be qualified without washing; the oxidation rate of sodium mercaptide in the alkali liquid is high, two-phase disturbance emulsification is tiny, and over 60% of the generated disulphide is separated and recycled; the content of disulphide in the regenerated alkali liquid can be guaranteed to be not over 100ppm, and the regenerated alkali liquid is not back-extracted into the product when in circular mercaptide removal; and the total sulfur of the product can be guaranteed to be stable without frequently replacing the alkali liquid, and the discharge amount of the alkali residues is reduced by over 50% in comparison with other technologies.
Description
Technical field
The utility model relates to petrochemical industry, relates in particular to the device of a kind of gasoline lighting end mercaptan removal and alkali liquid regeneration.
Background technology
In poor quality and high sulfuration along with crude oil, and society is to the day by day raising of Fuel Petroleum desulfurization requirement, require oil refining enterprise to improve constantly crude oil processing technology level, update the Fuel Petroleum sulfur removal technology, more will pay attention to the Sustainable development need of production of energy-saving and emission-reduction consumption reduction in the production process simultaneously.
European and American developed countries namely began to carry out the clean gasoline the Europe IV standard as far back as 2005, began to carry out Europe V standard in 2009, China also took the lead in 2011 in the ground such as Beijing, Shanghai enforcement state IV standard, require the motor benzine total sulfur to be no more than 50ppm, producing more, the clean gasoline of low sulfur content is that people are to the inevitable choice of living environment pay attention to day by day.
Tradition alkali cleaning extraction process can't satisfy current deep desulfurization of gasoline requirement, hydrogenating desulfurization then is the deep desulfuration technology of using at present comparative maturity and wideling popularize, but there is huge, the complicated operation of plant investment in hydrogenating desulfurization, the problem that the gasoline refining cost is high, but also have the shortcoming of losing gasoline octane rating.
Fushun Petrochemical Research Institute of SINOPEC is on the basis of hydrogenating desulfurization technology, by light, the last running cut point temperature of gasoline of selecting to suit, the lighting end higher to olefin(e) centent, that sulphur content is lower is carried out desulfurization with the method for alkali cleaning extracting and is processed, the last running that sulphur content is higher is carried out the hydrogenating desulfurization processing with the special desulfurization catalyst of developing, and two kinds of distillation gasolines after the desulfurization reconcile into gasoline product again.This technique has solved full distillation gasoline hydrogenation technique on the one hand to the problem of loss of octane number, and the cost of gasoline lighting end employing alkali cleaning extraction desulfurization alcohol greatly reduces the gasoline refining cost far below the hydrogenating desulfurization cost on the other hand.
Liquefied gas caustic wash desulfuration alcohol technology is very ripe, and what industrial application was more at present is packed extraction column and fiber film contactor two class mass transfer apparatuses, and the gasoline lighting end adopts the experimental study of caustic wash desulfuration alcohol and industrial application that ripe equipment and technology are not yet arranged.
The utility model content
The purpose of this utility model provides a kind of gasoline lighting end mercaptan removal and alkali liquid regeneration device, and present gasoline lighting end doctor process investment is huge solve to solve, complicated operation, the gasoline refining cost is high and the technical barrier such as loss gasoline octane rating.
The purpose of this utility model is achieved through the following technical solutions:
A kind of gasoline lighting end mercaptan removal and alkali liquid regeneration device, comprise static mixer, one-level liquid film alkali cleaning reactor, secondary liquid film alkali cleaning reactor, the coalescent device that takes off of alkali lye, alkali liquor oxidized knockout tower and liquid film extracting contactor, described static mixer links to each other with the caustic prescrub tank by pipeline, described caustic prescrub tank is connected with one-level alkali cleaning separating tank by one-level liquid film alkali cleaning reactor, described one-level liquid film alkali cleaning reactor is installed on the one-level alkali cleaning separating tank, the outlet of one-level alkali cleaning separating tank is connected with secondary alkali cleaning separating tank by secondary liquid film alkali cleaning reactor, secondary alkali cleaning separating tank is externally connected with the alkali lye coalescer, described one-level liquid film alkali cleaning reactor is provided with the circulation alkali liquor pump outward, and the circulation alkali liquid pump the other end separates the alkali lye outlet and is connected with the secondary alkali cleaning; Described secondary liquid film alkali cleaning reactor is connected with the outlet of regenerating alkali liquid pump with extracting separating tank alkali lye, and described regenerating alkali liquid pump is externally connected with fresh alkali lye feed-pipe; Outer alkali lye preheater and the catalyzer injector of being provided with of the alkali lye outlet of described one-level alkali cleaning separating tank, and be connected with the alkali lye import of described alkali liquor oxidized knockout tower, be provided with gas distributor, alkali liquor oxidized separation dividing plate and coalescent pack in the described alkali liquor oxidized knockout tower, described alkali liquor oxidized knockout tower is provided with disulphide discharge nozzle and tail gas discharge nozzle outward, the tail gas discharge nozzle is provided with tail gas and divides flow container, and described gas distributor is provided with compressed air pipe outward; Described alkali liquor oxidized knockout tower alkali lye outlet is connected with the extracting slurry tank with liquid film extracting contactor by the petroleum naphtha pipe, described liquid film extracting contactor is connected with the petroleum naphtha outlet of petroleum naphtha pump and liquid film extracting slurry tank, in the described extracting slurry tank coalescing-plate and dividing plate are installed, described petroleum naphtha pipe is provided with naphtha feed pipe and petroleum naphtha coalescer, and described petroleum naphtha coalescer is provided with Containing-sulfur Naphtha discharge nozzle and alkaline residue delivery pipe.
Further, described alkali lye coalescer bottom is connected with the alkaline residue tank, and top is provided with the clean petroleum product outlet; Be provided with coalescing-plate and dividing plate in the described extracting slurry tank.
The method of a kind of gasoline lighting end mercaptan removal and alkali liquid regeneration may further comprise the steps:
1) in static mixer, inputs fresh alkali lye by the caustic prescrub pump, pending gasoline stocks and alkali lye carry out shear-mixed reaction 0.1～2min in static mixer, the alkali lye mass rate is the 20-60%wt of quality of gasoline flow, the two is settlement separate 10～30min in the caustic prescrub tank, gasoline and alkali lye behind the caustic prescrub that obtains separating, alkali lye recycles, according to hydrogen sulfide in the product and the periodic replacement of phenol content;
2) behind the caustic prescrub gasoline by output tube and the alkali cleaning of secondary liquid film after alkali lye, in the one-level liquid film reactor, contact Laminar Flow with membrane-membrane, two-phase fully contacts and reacts, the alkali lye mass rate is the 10-40%wt of quality of gasoline flow, the two obtains one-level treated gasoline and one-level alkali lye at the settlement separate 30～60min of one-level alkali cleaning separating tank;
3) the one-level treated gasoline is by output tube and regeneration alkali lye, in the secondary liquid film reactor, contact Laminar Flow with membrane-membrane, two-phase fully contacts and reacts, the alkali lye mass rate is the 10-40%wt of quality of gasoline flow, the two obtains secondary treated gasoline and secondary alkali lye at the settlement separate 30～60min of one-level alkali cleaning separating tank;
4) one-level alkali lye force feed enters in the alkali liquor oxidized knockout tower, simultaneously pressurized air will be scattered in the alkali lye in the liquid oxidation knockout tower with the microvesicle form by gas distributor, the air consumption is 1-5 times of sodium mercaptides oxidation theory demands amount, sodium mercaptides oxide catalyst content in alkali lye is 50-200ppm, alkali liquor oxidized temperature is 20-70 ℃, airborne oxygen fully contacts with sodium mercaptides in the alkali lye and reacts and generates sodium hydroxide and disulphide, and dissolution of sodium hydroxide makes alkali lye obtain regeneration in alkali lye; The little alkali lye upper strata that floats over of disulphide density, alkali lye forms the alkali lye liquid film through the hydrophilic coalescent pack in disengaging zone, alkali lye fully contacts with the disulphide of layering, and the disulphide of emulsification is extracted in the disulphide of layering in the alkali lye, and disulphide content further reduces in the alkali lye;
5) alkali lye of oxidation separation disulphide and low-sulfur petroleum naphtha are by liquid film extracting contactor, the alkali lye mass rate is the 20-100%wt of petroleum naphtha mass rate, two-phase contacts Laminar Flow with membrane-membrane in liquid film extracting contactor, two-phase fully contacts, residual disulphide is extracted in the petroleum naphtha in the alkali lye, alkali lye and petroleum naphtha are at the settlement separate 30～90min of extracting slurry tank, alkali lye and Containing-sulfur Naphtha obtain regenerating, regeneration alkali lye is delivered to the secondary liquid film reactor by the regenerating alkali liquid pump, Containing-sulfur Naphtha 30-80% recycles, and 70-20% must remove carrying device behind the alkali lye by the petroleum naphtha coalescer;
6) described low-sulfur petroleum naphtha can be low-sulphur oil, chemical industry light oil, solvent oil or diesel oil.
Description of drawings
Fig. 1 is the structural representation of the described a kind of gasoline lighting end mercaptan removal of the utility model embodiment and alkali liquid regeneration device.
Among the figure:
1, static mixer; 2, caustic prescrub tank; 3, caustic prescrub pump; 4, one-level liquid film alkali cleaning reactor; 5, one-level alkali cleaning separating tank; 6, secondary liquid film alkali cleaning reactor; 7, secondary alkali cleaning separating tank; 8, alkali lye coalescer; 9, circulation alkali liquid pump; 10, alkali lye preheater; 11, catalyzer injector; 12, alkali liquor oxidized knockout tower; 13, gas distributor; 14, coalescent pack; 15, liquid film extracting contactor; 16, extracting slurry tank; 17, coalescing-plate; 18, dividing plate; 19, regenerating alkali liquid pump; 20, petroleum naphtha pump; 21, petroleum naphtha coalescer; 22, alkali liquor oxidized separation dividing plate; 23, tail gas divides flow container.
Embodiment
As shown in Figure 1, the described a kind of gasoline lighting end mercaptan removal of the utility model embodiment and alkali liquid regeneration device, comprise static mixer 1, one-level liquid film alkali cleaning reactor 4, secondary liquid film alkali cleaning reactor 6, the coalescent device 8 that takes off of alkali lye, alkali liquor oxidized knockout tower 12 and liquid film extracting contactor 15, described static mixer 1 links to each other with caustic prescrub tank 2 by pipeline, described caustic prescrub tank 2 is connected with one-level alkali cleaning separating tank 5 by one-level liquid film alkali cleaning reactor 4, described one-level liquid film alkali cleaning reactor 4 is installed on the one-level alkali cleaning separating tank 5, the outlet of one-level alkali cleaning separating tank 5 is connected with secondary alkali cleaning separating tank 7 by secondary liquid film alkali cleaning reactor 6, secondary alkali cleaning separating tank 7 is externally connected with alkali lye coalescer 8, the described one-level liquid film alkali cleaning reactor 4 outer circulation alkali liquor pumps 9 that are provided with, circulation alkali liquid pump 9 the other ends are connected with the outlet of secondary alkali cleaning separating tank 7 alkali lye; Described secondary liquid film alkali cleaning reactor 6 is connected with the outlet of regenerating alkali liquid pump 19 with extracting separating tank 16 alkali lye, and described regenerating alkali liquid pump 19 is externally connected with fresh alkali lye feed-pipe; Outer alkali lye preheater 10 and the catalyzer injector 11 of being provided with of the alkali lye outlet of described one-level alkali cleaning separating tank 5, and be connected with the alkali lye import of described alkali liquor oxidized knockout tower 12, be provided with gas distributor 13, alkali liquor oxidized separation dividing plate 22 and coalescent pack 14 in the described alkali liquor oxidized knockout tower 12, described alkali liquor oxidized knockout tower 12 outer disulphide discharge nozzle and the tail gas discharge nozzles of being provided with, the tail gas discharge nozzle is provided with tail gas and divides flow container 23, the described gas distributor 13 outer compressed air pipes that are provided with; Described alkali liquor oxidized knockout tower 12 alkali lye outlet is connected with extracting slurry tank 16 with liquid film extracting contactor 15 by the petroleum naphtha pipe, described liquid film extracting contactor 15 is connected with the petroleum naphtha outlet of petroleum naphtha pump 20 and liquid film extracting slurry tank 16, coalescing-plate 17 and dividing plate 18 are installed in the described extracting slurry tank 16, described petroleum naphtha pipe is provided with naphtha feed pipe and petroleum naphtha coalescer 21, and described petroleum naphtha coalescer 21 is provided with Containing-sulfur Naphtha discharge nozzle 42 and alkaline residue delivery pipe 43.Described alkali lye coalescer 8 bottoms are connected with the alkaline residue tank, and top is provided with the clean petroleum product outlet; Be provided with coalescing-plate 17 and dividing plate 18 in the described extracting slurry tank 16.
The method of the utility model embodiment described gasoline lighting end mercaptan removal and alkali liquid regeneration may further comprise the steps:
1) in static mixer, inputs fresh alkali lye by the caustic prescrub pump, pending gasoline stocks and alkali lye carry out shear-mixed reaction 0.1～2min in static mixer, the alkali lye mass rate is the 20-60%wt of quality of gasoline flow, the two is settlement separate 10～30min in the caustic prescrub tank, gasoline and alkali lye behind the caustic prescrub that obtains separating, alkali lye recycles, according to hydrogen sulfide in the product and the periodic replacement of phenol content;
2) behind the caustic prescrub gasoline by output tube and the alkali cleaning of secondary liquid film after alkali lye, in the one-level liquid film reactor, contact Laminar Flow with membrane-membrane, two-phase fully contacts and reacts, the alkali lye mass rate is the 10-40%wt of quality of gasoline flow, the two obtains one-level treated gasoline and one-level alkali lye at the settlement separate 30～60min of one-level alkali cleaning separating tank;
3) the one-level treated gasoline is by output tube and regeneration alkali lye, in the secondary liquid film reactor, contact Laminar Flow with membrane-membrane, two-phase fully contacts and reacts, the alkali lye mass rate is the 10-40%wt of quality of gasoline flow, the two obtains secondary treated gasoline and secondary alkali lye at the settlement separate 30～60min of one-level alkali cleaning separating tank;
4) one-level alkali lye force feed enters in the alkali liquor oxidized knockout tower, simultaneously pressurized air will be scattered in the alkali lye in the liquid oxidation knockout tower with the microvesicle form by gas distributor, the air consumption is 1-5 times of sodium mercaptides oxidation theory demands amount, sodium mercaptides oxide catalyst content in alkali lye is 50-200ppm, alkali liquor oxidized temperature is 20-70 ℃, airborne oxygen fully contacts with sodium mercaptides in the alkali lye and reacts and generates sodium hydroxide and disulphide, and dissolution of sodium hydroxide makes alkali lye obtain regeneration in alkali lye; The little alkali lye upper strata that floats over of disulphide density, alkali lye forms the alkali lye liquid film through the hydrophilic coalescent pack in disengaging zone, alkali lye fully contacts with the disulphide of layering, and the disulphide of emulsification is extracted in the disulphide of layering in the alkali lye, and disulphide content further reduces in the alkali lye;
5) alkali lye of oxidation separation disulphide and low-sulfur petroleum naphtha are by liquid film extracting contactor, the alkali lye mass rate is the 20-100%wt of petroleum naphtha mass rate, two-phase contacts Laminar Flow with membrane-membrane in liquid film extracting contactor, two-phase fully contacts, residual disulphide is extracted in the petroleum naphtha in the alkali lye, alkali lye and petroleum naphtha are at the settlement separate 30～90min of extracting slurry tank, alkali lye and Containing-sulfur Naphtha obtain regenerating, regeneration alkali lye is delivered to the secondary liquid film reactor by the regenerating alkali liquid pump, Containing-sulfur Naphtha 30-80% recycles, and 70-20% must remove carrying device behind the alkali lye by the petroleum naphtha coalescer;
6) described low-sulfur petroleum naphtha can be low-sulphur oil, chemical industry light oil, solvent oil or diesel oil.
Application example
Certain company adopts the utility model technology, has built up cover gasoline lighting end mercaptan removal and an alkali liquid regeneration device:
Gasoline lighting end processing power: 25.8t/h; Turndown ratio: 50-110%; Point: 30-68 ℃ of gasoline lighting end distillation; Gasoline lighting end main character: hydrogen sulfide＜30ppm, mercaptan＜210ppm, total sulfur＜270ppm, motion device pressure 0.6-0.8MPaG, temperature 30-45 ℃; Process operation parameter: caustic prescrub flux of alkaline liquor 6t/h, mercaptan removal alkali lye circular flow 4t/h, catalyst content 100-150ppm, 30-50 ℃ of alkaline residue oxidizing temperature, compressed air require 30-40Nm
3/ h, petroleum naphtha circular flow 12-16t/h, petroleum naphtha is changed flow 2-3t/h; Device operation result: refining petroleum naphtha: hydrogen sulfide does not measure, mercaptans content 2-8ppm, doctor test detect as without, copper corrosion 1a other situation by, water-soluble soda acid: caustic prescrub is changed per month 15 tons of alkali lye, operation and is not changed mercaptan removal agent alkali half a year, reclaims 2 tons of disulphide per month.
Although below only described embodiment example of the present utility model, it will be understood by those of skill in the art that these only illustrate, protection domain of the present utility model is limited by appended claims.Those skilled in the art can make various changes or modifications to these embodiments under the prerequisite that does not deviate from principle of the present utility model and essence, but these changes or modification all fall into protection domain of the present utility model.
Claims (2)
1. a gasoline lighting end mercaptan removal and alkali liquid regeneration device, comprise static mixer (1), one-level liquid film alkali cleaning reactor (4), secondary liquid film alkali cleaning reactor (6), the coalescent device (8) that takes off of alkali lye, alkali liquor oxidized knockout tower (12) and liquid film extracting contactor (15), it is characterized in that: described static mixer (1) links to each other with caustic prescrub tank (2) by pipeline, caustic prescrub tank (2) is connected with one-level alkali cleaning separating tank (5) by one-level liquid film alkali cleaning reactor (4), described one-level liquid film alkali cleaning reactor (4) is installed on the one-level alkali cleaning separating tank (5), the outlet of one-level alkali cleaning separating tank (5) is connected with secondary alkali cleaning separating tank (7) by secondary liquid film alkali cleaning reactor (6), secondary alkali cleaning separating tank (7) is externally connected with alkali lye coalescer (8), the outer circulation alkali liquor pump (9) that is provided with of described one-level liquid film alkali cleaning reactor (4), circulation alkali liquid pump (9) the other end is connected with the outlet of secondary alkali cleaning separating tank (7) alkali lye; Described secondary liquid film alkali cleaning reactor (6) is connected with the outlet of regenerating alkali liquid pump (19) with extracting separating tank (16) alkali lye, and described regenerating alkali liquid pump (19) is externally connected with fresh alkali lye feed-pipe; Being provided with alkali lye preheater (10) outside the alkali lye outlet of described one-level alkali cleaning separating tank (5) is connected with catalyzer injector (11) and with the alkali lye import of described alkali liquor oxidized knockout tower (12), be provided with gas distributor (13), alkali liquor oxidized separation dividing plate (22) and coalescent pack (14) in the described alkali liquor oxidized knockout tower (12), outer disulphide discharge nozzle and the tail gas discharge nozzle of being provided with of described alkali liquor oxidized knockout tower (12), this tail gas discharge nozzle is provided with tail gas and divides flow container (23), the outer compressed air pipe that is provided with of described gas distributor (13); The alkali lye outlet of described alkali liquor oxidized knockout tower (12) is connected with extracting slurry tank (16) with liquid film extracting contactor (15) by the petroleum naphtha pipe, described liquid film extracting contactor (15) connects the petroleum naphtha outlet of petroleum naphtha pump (20) and liquid film extracting slurry tank (16), coalescing-plate (17) and dividing plate (18) are installed in the described extracting slurry tank (16), described petroleum naphtha pipe is provided with naphtha feed pipe and petroleum naphtha coalescer (21), and described petroleum naphtha coalescer (21) is provided with Containing-sulfur Naphtha discharge nozzle (42) and alkaline residue delivery pipe (43).
2. a kind of gasoline lighting end mercaptan removal according to claim 1 and alkali liquid regeneration device is characterized in that: described alkali lye coalescer (8) bottom is connected with the alkaline residue tank, and described alkali lye coalescer (8) top is provided with clean petroleum product and exports; Be provided with coalescing-plate (17) and dividing plate (18) in the described extracting slurry tank (16).
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220385221 CN202808717U (en) | 2012-08-03 | 2012-08-03 | Gasoline light fraction mercaptan removal and alkali liquid regeneration device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220385221 CN202808717U (en) | 2012-08-03 | 2012-08-03 | Gasoline light fraction mercaptan removal and alkali liquid regeneration device |
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| CN202808717U true CN202808717U (en) | 2013-03-20 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757809A (en) * | 2012-08-03 | 2012-10-31 | 宁波中一石化科技有限公司 | Mercaptan removal and lye regeneration device and method for gasoline light fractions |
| WO2018118689A1 (en) | 2016-12-21 | 2018-06-28 | Uop Llc | Process for oxidizing thiol compounds in a single vessel |
| CN110251991A (en) * | 2019-08-02 | 2019-09-20 | 青岛华友恒新能源材料技术研究院有限公司 | A kind of liquid-liquid extraction phase-splitter |
| CN111116775A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Process and apparatus for preparing low viscosity poly α -olefins |
-
2012
- 2012-08-03 CN CN 201220385221 patent/CN202808717U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757809A (en) * | 2012-08-03 | 2012-10-31 | 宁波中一石化科技有限公司 | Mercaptan removal and lye regeneration device and method for gasoline light fractions |
| CN102757809B (en) * | 2012-08-03 | 2015-03-18 | 宁波中一石化科技有限公司 | Mercaptan removal and lye regeneration device and method for gasoline light fractions |
| WO2018118689A1 (en) | 2016-12-21 | 2018-06-28 | Uop Llc | Process for oxidizing thiol compounds in a single vessel |
| EP3559160A4 (en) * | 2016-12-21 | 2020-07-15 | Uop Llc | Process for oxidizing thiol compounds in a single vessel |
| CN111116775A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Process and apparatus for preparing low viscosity poly α -olefins |
| CN111116775B (en) * | 2018-10-30 | 2022-10-21 | 中国石油化工股份有限公司 | Process and apparatus for producing low viscosity polyalphaolefin |
| CN110251991A (en) * | 2019-08-02 | 2019-09-20 | 青岛华友恒新能源材料技术研究院有限公司 | A kind of liquid-liquid extraction phase-splitter |
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| C14 | Grant of patent or utility model | ||
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| C56 | Change in the name or address of the patentee | ||
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Address after: 315040, Zhejiang, Ningbo province National hi tech Zone Lingyun road 1177 Lingyun Industrial Park, building 10, north 2 floor Patentee after: NINGBO ZHONGYI PETROCHEMICAL TECHNOLOGY CO., LTD. Address before: 315040, Zhejiang, Ningbo province National hi tech Zone Lingyun road 1177 Lingyun Industrial Park, building 10, north 2 floor Patentee before: Ningbo Zhongyi Petrochemical Technology Co., Ltd. |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20130320 Effective date of abandoning: 20150318 |
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| RGAV | Abandon patent right to avoid regrant |