CN205443218U - Novel natural qi exhaustion heavy hydrocarbon device - Google Patents
Novel natural qi exhaustion heavy hydrocarbon device Download PDFInfo
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- CN205443218U CN205443218U CN201620259060.XU CN201620259060U CN205443218U CN 205443218 U CN205443218 U CN 205443218U CN 201620259060 U CN201620259060 U CN 201620259060U CN 205443218 U CN205443218 U CN 205443218U
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- heavy hydrocarbon
- natural gas
- lng
- scrubbing tower
- stabilizer
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Abstract
The utility model relates to a novel natural qi exhaustion heavy hydrocarbon device, the device include heat exchanger (1), LNG flash tank (2), take off heavy hydrocarbon scrubbing tower (3), heavy hydrocarbon stabilizer (4), LNG circulating pump (5) and MR separator (6), take off the export of heavy hydrocarbon scrubbing tower (3) and the entry linkage of LNG flash tank (2), the export of LNG flash tank (2) pass through LNG circulation canal (26) in proper order with LNG circulating pump (5) with take off the entry linkage of heavy hydrocarbon scrubbing tower (3), the export of taking off heavy hydrocarbon scrubbing tower (3) still through heavy hydrocarbon circulation canal (9) the entry linkage with heavy hydrocarbon stabilizer (4), the export of heavy hydrocarbon stabilizer (4) pass through the entry linkage of natural gas passageway III (17) and LNG flash tank (2). The utility model has the advantages of strong operability, low in production cost, reduction energy consumption, economic benefits are good.
Description
Technical field
This utility model relates to natural gas purification technical field, particularly a kind of novel natural gas de-heavy hydrocarbon apparatus.
Background technology
The natural gas being presently used for natural gas liquefaction device mainly has conventional gas (oil-gas reservoir) and Unconventional forage (coal bed gas, shale gas etc.).In gas deliquescence process, owing to feed gas composition is relative complex, heavy hydrocarbons content changes greatly, heavy hydrocarbons content in liquefaction ice chest can be caused at low ambient temperatures to increase, if not in time heavy hydrocarbon being carried out removing process, will result in ice chest and line clogging and the problem such as freeze, therefore, it is necessary to be isolated removing before condensation liquefaction or in condensation process.
At present, conventional de-heavy hydrocarbon technology mainly has: the methods such as active carbon adsorption, low temperature heavy hydrocarbon washing method.Active carbon adsorption is the Adsorption utilizing the high characterization of adsorption under the strong and low dividing potential drop of activated carbon Molecular Adsorption selective power to carry out heavy hydrocarbon.China Patent No.: CN201320862991.5 discloses a kind of natural gas de-heavy hydrocarbon apparatus, technique described in this patent uses the heavy hydrocarbon in the composite bed removing unstripped gas of the adsorbent such as activated carbon, water-fast silica-gel mixture layer, and uses three tower equipressure adsorption process to take off the regeneration gas of heavy hydrocarbon tower from unstripped gas.But, this technique is limited by solid absorbent saturation, absorption content and regeneration level, is unsuitable for high throughput and the high device of heavy hydrocarbons content；Additionally, this technique is additionally arranged regeneration gas heater, and the regeneration gas of this device is obtained by unstripped gas blood pressure lowering, so causes whole unstripped gas and enters the pressure decline of ice chest, adds the energy consumption in liquefaction process.Washing method is to utilize heavy hydrocarbon at C2~i-C5There is higher dissolubility, and arrive a kind of method of removing heavy hydrocarbon.China Patent No.: CN1743418A proposes the method for removing heavy hydrocarbon in natural gas by adsorption of heavy hydrocarbon, and the method uses unstripped gas self to be condensed out heavy hydrocarbon (mainly C2~i-C5) carry out the heavy hydrocarbon in washing material gas.But, owing to washing method removes heavy hydrocarbon, affected relatively big, as C in feed gas composition by feed gas composition2~i-C5Time less, washing method effect is undesirable, can not thoroughly remove heavy hydrocarbon.
Utility model content
The purpose of this utility model is to overcome the shortcoming of prior art, it is provided that a kind of novel natural gas de-heavy hydrocarbon apparatus, and it is low that this device has stronger operability, production cost；Again by cold recovery while removing heavy hydrocarbon, reduce energy consumption；Increase heavy hydrocarbon stabilizer and tail gas is re-liquefied, C during beneficially recovery is dissolved in heavy hydrocarbon1~C4, bigger economic benefit can be obtained.
nullThe purpose of this utility model is achieved through the following technical solutions: a kind of novel natural gas de-heavy hydrocarbon apparatus，It includes heat exchanger、LNG flash tank、De-heavy hydrocarbon scrubbing tower、Heavy hydrocarbon stabilizer、LNG circulating pump and MR separator，Natural gas passage I it is provided with in described heat exchanger、Natural gas passage II、Natural gas passage III and heavy hydrocarbon circulation canal，Described heat exchanger is outside equipped with natural gas passage IV，Described natural gas passage I and natural gas passage IV all entrances with de-heavy hydrocarbon scrubbing tower are connected，The outlet of described de-heavy hydrocarbon scrubbing tower is connected by the entrance of natural gas passage II and LNG flash tank，The outlet of described LNG flash tank by LNG circulation canal successively entrance with LNG circulating pump and de-heavy hydrocarbon scrubbing tower be connected，The exit of described LNG flash tank is also associated with LNG output channel and BOG output channel，The outlet of described de-heavy hydrocarbon scrubbing tower is connected also by the entrance of heavy hydrocarbon circulation canal with heavy hydrocarbon stabilizer，The outlet of described heavy hydrocarbon stabilizer is connected by the entrance of natural gas passage III and LNG flash tank，The exit of described heavy hydrocarbon stabilizer is also associated with heavy hydrocarbon output channel.
Preferably, gas phase coolant channel, gas-liquid mixed phase coolant channel and liquid phase coolant channel it is additionally provided with in described heat exchanger, described gas phase coolant channel is connected with the entrance of MR separator, the outlet of MR separator is connected with gas-liquid mixed phase coolant channel, and described liquid phase coolant channel connects with gas-liquid mixed phase coolant channel.
Preferably, the top of described heavy hydrocarbon stabilizer is provided with condenser, and the bottom of described heavy hydrocarbon stabilizer is provided with reboiler.
Preferably, described natural gas passage IV is provided with regulation valve a and temperature digital controller.
Preferably, described heavy hydrocarbon circulation canal is provided with regulation valve h and liquid level digitial controller B.
Preferably, described LNG output channel is provided with regulation valve f and liquid level digitial controller A.
Preferably, described LNG circulation canal is provided with regulation valve g and traffic figure controller.
Preferably, described LNG flash tank is provided with demister.
Preferably, described de-heavy hydrocarbon scrubbing tower is provided with demister.
Preferably, described de-heavy hydrocarbon scrubbing tower is packed tower or plate column.
Preferably, described heavy hydrocarbon stabilizer is packed tower or plate column.
Preferably, described reboiler is built-in reboiler, kettle type reboiler or thermosyphon reboiler.
Preferably, described heat exchanger is plate type heat exchanger, wound tube heat exchanger or shell-and-tube heat exchanger.
Preferably, described natural gas passage I, natural gas passage II, natural gas passage III, heavy hydrocarbon circulation canal, gas phase coolant channel, gas-liquid mixed phase coolant channel and liquid phase coolant channel are parallel to each other.
Preferably, described gas phase coolant channel and liquid phase coolant channel are respectively high pressure vapor coolant channel and high-pressure liquid phase coolant channel.
The method utilizing above-mentioned novel natural gas de-heavy hydrocarbon apparatus to carry out de-hydrocarbon comprises the following steps:
S1, through deacidification, be dried qualified natural gas be divided into two strands at A point, carrying out pre-cooling in natural gas passage I in first strand of entrance heat exchanger, the second stock-traders' know-how enters in de-heavy hydrocarbon scrubbing tower after being converged by the first of pre-cooling strand of natural gas in crossing natural gas passage IV and entering heat exchanger；
S2, natural gas enter in natural gas passage II from the output of de-heavy hydrocarbon scrubbing tower top cool down, condense, liquefy after enter in LNG flash tank；
S3, the isolated BOG of LNG flash tank through BOG output channel export；The LNG part obtained exports through LNG output channel, and another part sends into de-heavy hydrocarbon scrubbing tower top through the pressurization of LNG circulating pump；
S4, pressurized feeding take off the heavy hydrocarbon that LNG in heavy hydrocarbon scrubbing tower obtains after described de-heavy hydrocarbon scrubbing tower processes and enter heavy hydrocarbon circulation canal and carry out re-heat, then in heavy hydrocarbon circulation canal is transported to heavy hydrocarbon stabilizer；
S5, the C obtained through the process of heavy hydrocarbon stabilizer1~C4Be cooled through natural gas passage III, condense, liquefy after enter LNG flash tank together with the liquefied natural gas obtained in step S2, process, through heavy hydrocarbon stabilizer, the C that obtains5 +Export through heavy hydrocarbon output channel.
Preferably, being provided with gas phase coolant channel, gas-liquid mixed phase coolant channel and liquid phase coolant channel in described heat exchanger, gas phase and liquid phase that described gas phase cryogen obtains after sequentially entering the interior cooling of gas phase coolant channel, entrance MR separator gas-liquid separation are transported in gas-liquid mixed phase coolant channel；Also in gas-liquid mixed phase coolant channel after cooling in liquid phase cryogen entrance liquid phase coolant channel.
Preferably, described step S5 processes the C obtained through heavy hydrocarbon stabilizer1~C4Enter natural gas passage III be cooled, condense, liquefy after also can the most defeated another use.
This utility model has the advantage that
1, effectively prevent Cold box blocking and freezing: this utility model squeezes into de-heavy hydrocarbon scrubbing tower top after using product LNG pressurized, the unstripped gas entering de-heavy hydrocarbon wash tower bottoms is washed, effectively the heavy hydrocarbon in unstripped gas can be removed, prevent Cold box blocking and freezing；
2, reduce energy consumption, reduce cost of investment: in this utility model, the temperature of the de-heavy hydrocarbon scrubbing tower of unstripped gas entrance can be adjusted by regulation valve a, instead of the vaporizer that conventional heavy hydrocarbon washing method is used, and de-heavy hydrocarbon scrubbing tower top uses the LNG of low temperature as cleaning mixture, instead of the condenser of conventional heavy hydrocarbon washing method, compared with conventional heavy hydrocarbon washing method device, liquefaction plant total energy consumption reduces by 5% ~ 8%, reduces cost of investment；And again by cold recovery while removing heavy hydrocarbon, reduce energy consumption further；
3, increasing obtains side-product, economy reliably: this utility model have employed heavy hydrocarbon stabilizer and separated by the heavy hydrocarbon after cold washing, beneficially reclaims the C being dissolved in heavy hydrocarbon1~C4, obtain light oil side-product, economical reliable, bigger economic benefit can be obtained；
4, liquefied rate is improved: heavy hydrocarbon stabilizer top light component out has been carried out reclaiming liquefaction by this utility model, improves the liquefied fraction of natural gas, can obtain bigger economic benefit；
5 additionally, this device also has the advantages such as stronger operability, production cost be low.
Accompanying drawing explanation
Fig. 1 is the structural representation in this utility model detailed description of the invention；
nullIn figure: 1-heat exchanger，2-LNG flash tank，3-takes off heavy hydrocarbon scrubbing tower，4-heavy hydrocarbon stabilizer，5-LNG circulating pump，6-MR separator，7-regulates valve a，8-natural gas passage IV，9-heavy hydrocarbon circulation canal，10-natural gas passage I，11-gas phase coolant channel，12-gas-liquid mixed phase coolant channel，13-liquid phase coolant channel，14-regulates valve b，15-regulates valve c，16-natural gas passage II，17-natural gas passage III，18-regulates valve d，19-regulates valve e，20-liquid level digitial controller A，21-regulates valve f，22-LNG output channel，23-regulates valve g，24-traffic figure controller，25-BOG output channel，26-LNG circulation canal，27-regulates valve h，28-liquid level digitial controller B，29-temperature digital controller，30-heavy hydrocarbon output channel，31-regulates valve i，32-reboiler，33-condenser，34-regulates valve j.
Detailed description of the invention
Below in conjunction with the accompanying drawings this utility model is further described, but protection domain of the present utility model is not limited to the following stated.
As it is shown in figure 1, a kind of novel natural gas de-heavy hydrocarbon apparatus, it includes heat exchanger 1, LNG flash tank 2, de-heavy hydrocarbon scrubbing tower 3, heavy hydrocarbon stabilizer 4, LNG circulating pump 5 and MR separator 6.Described heat exchanger 1 is plate type heat exchanger, and described de-heavy hydrocarbon scrubbing tower 3 is packed tower, and described heavy hydrocarbon stabilizer 4 is plate column, and described LNG flash tank 2 is provided with demister in de-heavy hydrocarbon scrubbing tower 3 respectively.
Parallel natural gas passage I10, natural gas passage II16, natural gas passage III17, heavy hydrocarbon circulation canal 9, gas phase coolant channel 11, gas-liquid mixed phase coolant channel 12 and liquid phase coolant channel 13 it is provided with in described heat exchanger 1, described heat exchanger 1 is outside equipped with natural gas passage IV 8, described gas phase coolant channel 11 and liquid phase coolant channel 13 and is respectively high pressure vapor coolant channel and high-pressure liquid phase coolant channel.
LNG entrance, BOG gaseous phase outlet and LNG liquid-phase outlet B it is provided with on described LNG flash tank 2；LNG entrance D, gas inlet E, heavy hydrocarbon outlet G and gas outlet F are set on described de-heavy hydrocarbon scrubbing tower 3；Heavy hydrocarbon entrance H, light oil outlet I and gas outlet J it is provided with on described heavy hydrocarbon stabilizer 4；Cryogen entrance K, top gas phase cryogen outlet L and bottom liquid phases cryogen outlet M it is provided with on described MR separator 6.
Described natural gas passage I10 and natural gas passage IV 8 all gas inlet E with de-heavy hydrocarbon scrubbing tower 3 are connected, and natural gas passage IV 8 is provided with regulation valve a7 and temperature digital controller 29；The top gas outlet F of described de-heavy hydrocarbon scrubbing tower 3 is connected by the LNG entrance of natural gas passage II16 and LNG flash tank 2, and natural gas passage II16 is provided with regulation valve d18.The LNG liquid-phase outlet B of described LNG flash tank 2 is connected with the LNG entrance D of LNG circulating pump 5 and de-heavy hydrocarbon scrubbing tower 3 successively by LNG circulation canal 26, and described LNG circulation canal 26 is provided with regulation valve g23 and traffic figure controller 24；It is also associated with LNG output channel 22 at the LNG liquid-phase outlet B of described LNG flash tank 2, LNG output channel 22 is provided with regulation valve f21 and liquid level digitial controller A20；The top BOG gaseous phase outlet of LNG flash tank 2 connects BOG output channel 25.
The bottom heavy hydrocarbon outlet G of described de-heavy hydrocarbon scrubbing tower 3 is connected with the heavy hydrocarbon entrance H of heavy hydrocarbon stabilizer 4 also by heavy hydrocarbon circulation canal 9, and heavy hydrocarbon circulation canal 9 is provided with regulation valve h27 and liquid level digitial controller B28.The top gas outlet J of described heavy hydrocarbon stabilizer 4 is connected by the LNG entrance of natural gas passage III17 and LNG flash tank 2, and natural gas passage III17 is provided with regulation valve e19 and regulation valve j34；It is also associated with heavy hydrocarbon output channel 30 at the bottom light oil outlet I of described heavy hydrocarbon stabilizer 4, heavy hydrocarbon output channel 30 is provided with regulation valve i31；The top of heavy hydrocarbon stabilizer 4 is provided with condenser 33, and the bottom of heavy hydrocarbon stabilizer 4 is provided with reboiler 32, and reboiler 32 is built-in reboiler.Described gas phase coolant channel 11 is connected with the cryogen entrance K of MR separator 6, regulation valve c15 it is provided with on gas phase coolant channel 11, the bottom liquid phases cryogen outlet M and top gas phase cryogen outlet L of MR separator 6 are all connected with gas-liquid mixed phase coolant channel 12, described liquid phase coolant channel 13 connects with gas-liquid mixed phase coolant channel 12, and liquid phase coolant channel 13 is provided with regulation valve b14.
The method utilizing above-mentioned novel natural gas de-heavy hydrocarbon apparatus to carry out de-hydrocarbon comprises the following steps:
S1, through deacidification, be dried qualified natural gas be divided into two strands at A point, natural gas passage I10 in first strand of entrance heat exchanger 1 is carried out pre-be cooled to-70 ~-35 DEG C, second stock-traders' know-how enters in de-heavy hydrocarbon scrubbing tower 3 from the gas inlet E of de-heavy hydrocarbon scrubbing tower 3 after being converged by the first of pre-cooling strand of natural gas in crossing natural gas passage IV 8 and entering heat exchanger 1, unstripped gas is entered the temperature of de-heavy hydrocarbon scrubbing tower 3 and can be adjusted by regulation valve a7, temperature in de-heavy hydrocarbon scrubbing tower 3 is-65 ~ 0 DEG C, the operation pressure 1 ~ 10Mpag of de-heavy hydrocarbon scrubbing tower 3；Gas phase coolant channel 11, gas-liquid mixed phase coolant channel 12 and liquid phase coolant channel 13 it is provided with in described heat exchanger 1, described high pressure vapor cryogen is cooled to uniform temperature in entering gas phase coolant channel 11, again after overregulating valve c15 throttling, gas phase and liquid phase, gas phase and liquid phase that entrance MR separator 6 gas-liquid separation obtains enter in gas-liquid mixed phase coolant channel 12 from the different mouths of pipe；High-pressure liquid phase cryogen is cooled to uniform temperature in entering liquid phase coolant channel 13, then is adjusted after valve b14 throttles also in gas-liquid mixed phase coolant channel 13；
S2, natural gas enter in natural gas passage II16 from de-heavy hydrocarbon scrubbing tower 3 top gas outlet F output and cool down, condense, liquefy, then after being adjusted valve d18 throttling, enter in LNG flash tank 2；
S3, export through BOG output channel 25 at the isolated BOG of LNG flash tank 2；The LNG part obtained exports through LNG output channel 22, and another part sends into de-heavy hydrocarbon scrubbing tower 3 top through LNG circulating pump 5 pressurization, and the amount entering de-heavy hydrocarbon scrubbing tower 3 can be regulated by regulation valve g23；
S4, pressurized feeding take off the heavy hydrocarbon that LNG in heavy hydrocarbon scrubbing tower 3 obtains after described de-heavy hydrocarbon scrubbing tower 3 processes and enter heavy hydrocarbon circulation canal 9 from the outlet G output of bottom heavy hydrocarbon and carry out re-heat, are then transported to the middle part of heavy hydrocarbon stabilizer 4 through heavy hydrocarbon circulation canal 9；The operation pressure 0.2Mpag ~ 3.5Mpag of heavy hydrocarbon stabilizer 4, the operation temperature of heavy hydrocarbon stabilizer 4 tower top-35 ~ 40 DEG C, operate temperature 45 ~ 150 DEG C at the bottom of tower；
S5, the C obtained through heavy hydrocarbon stabilizer 4 process1~C4Enter in natural gas passage III17 through top gas outlet J output and cool down, condense, liquefy, then after being adjusted valve 19e throttling, enter LNG flash tank 2 together with the liquefied natural gas obtained in step S2, process the C obtained through heavy hydrocarbon stabilizer 45 +Export through heavy hydrocarbon output channel 30, be so possible not only to obtain side-product light oil, improve again liquefied rate；Additionally, process the C obtained through heavy hydrocarbon stabilizer 41~C4Enter natural gas passage III17 be cooled, condense, liquefy after also can the most defeated another use.
Claims (8)
- null1. a novel natural gas de-heavy hydrocarbon apparatus，It is characterized in that，It includes heat exchanger (1)、LNG flash tank (2)、De-heavy hydrocarbon scrubbing tower (3)、Heavy hydrocarbon stabilizer (4)、LNG circulating pump (5) and MR separator (6)，It is provided with natural gas passage I(10) in described heat exchanger (1)、Natural gas passage II(16)、Natural gas passage III(17) and heavy hydrocarbon circulation canal (9)，Described heat exchanger (1) is outside equipped with natural gas passage IV (8)，Described natural gas passage I(10) and natural gas passage IV (8) all entrances with de-heavy hydrocarbon scrubbing tower (3) be connected，The outlet of described de-heavy hydrocarbon scrubbing tower (3) is by natural gas passage II(16) it is connected with the entrance of LNG flash tank (2)，The outlet of described LNG flash tank (2) by LNG circulation canal (26) successively entrance with LNG circulating pump (5) and de-heavy hydrocarbon scrubbing tower (3) be connected，The exit of described LNG flash tank (2) is also associated with LNG output channel (22) and BOG output channel (25)，The outlet of described de-heavy hydrocarbon scrubbing tower (3) is connected also by the entrance of heavy hydrocarbon circulation canal (9) with heavy hydrocarbon stabilizer (4)，The outlet of described heavy hydrocarbon stabilizer (4) is by natural gas passage III(17) it is connected with the entrance of LNG flash tank (2)，The exit of described heavy hydrocarbon stabilizer (4) is also associated with heavy hydrocarbon output channel (30).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterized in that, gas phase coolant channel (11), gas-liquid mixed phase coolant channel (12) and liquid phase coolant channel (13) it is additionally provided with in described heat exchanger (1), described gas phase coolant channel (11) is connected with the entrance of MR separator (6), the outlet of MR separator (6) is connected with gas-liquid mixed phase coolant channel (12), and described liquid phase coolant channel (13) connects with gas-liquid mixed phase coolant channel (12).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that the top of described heavy hydrocarbon stabilizer (4) is provided with condenser (33), and the bottom of described heavy hydrocarbon stabilizer (4) is provided with reboiler (32).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that be provided with regulation valve a(7 on described natural gas passage IV (8)) and temperature digital controller (29).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that be provided with regulation valve h(27 on described heavy hydrocarbon circulation canal (9)) and liquid level digitial controller B(28).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that be provided with regulation valve f(21 in described LNG output channel (22)) and liquid level digitial controller A(20).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that be provided with regulation valve g(23 on described LNG circulation canal (26)) and traffic figure controller (24).
- A kind of novel natural gas de-heavy hydrocarbon apparatus the most according to claim 1, it is characterised in that be provided with demister in described LNG flash tank (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620259060.XU CN205443218U (en) | 2016-03-31 | 2016-03-31 | Novel natural qi exhaustion heavy hydrocarbon device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620259060.XU CN205443218U (en) | 2016-03-31 | 2016-03-31 | Novel natural qi exhaustion heavy hydrocarbon device |
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| Publication Number | Publication Date |
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| CN205443218U true CN205443218U (en) | 2016-08-10 |
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| CN201620259060.XU Withdrawn - After Issue CN205443218U (en) | 2016-03-31 | 2016-03-31 | Novel natural qi exhaustion heavy hydrocarbon device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105695015A (en) * | 2016-03-31 | 2016-06-22 | 成都深冷液化设备股份有限公司 | Novel natural gas heavy hydrocarbon removal device and method |
-
2016
- 2016-03-31 CN CN201620259060.XU patent/CN205443218U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105695015A (en) * | 2016-03-31 | 2016-06-22 | 成都深冷液化设备股份有限公司 | Novel natural gas heavy hydrocarbon removal device and method |
| CN105695015B (en) * | 2016-03-31 | 2018-09-25 | 成都深冷液化设备股份有限公司 | A kind of novel natural gas de-heavy hydrocarbon apparatus and method |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20160810 Effective date of abandoning: 20180925 |
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| AV01 | Patent right actively abandoned |