CN205079543U - Device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen - Google Patents
Device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen Download PDFInfo
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- CN205079543U CN205079543U CN201520715331.3U CN201520715331U CN205079543U CN 205079543 U CN205079543 U CN 205079543U CN 201520715331 U CN201520715331 U CN 201520715331U CN 205079543 U CN205079543 U CN 205079543U
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Abstract
The utility model relates to a device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen, the device include air generation system, front end precooling purification system and cold box. The utility model discloses make full use of cryogenic rectification method, one set of device obtains low -purity oxygen, high purity oxygen and nitrogen simultaneously to and the liquid product, compare with adopting pressure swing adsorption to obtain low -purity oxygen, high purity oxygen, high -purity nitrogen, install small in quantityly, the energy consumption is low, and economic nature is good, and the product extraction percentage is up to more than 99%, and compression in product oxygen adopts economizes the deoxidation press, and the security is good, the coloured smelting of the specially adapted sky branch of forming a complete set.
Description
Technical field
The utility model relates to air separation field, particularly relates to the device of a kind of cryogenic separation and production low purity oxygen, high purity oxygen and nitrogen.
Background technology
Along with the fast development of all trades and professions, the type requirements of industrial gasses oxygen, nitrogen is also got more and more, only require that single purity oxygen product (need not produce the one in high purity oxygen or low purity oxygen) with traditional industries, some emerging industries are as nonferrous smelting, occurred requiring to produce low purity oxygen, high purity oxygen, high-purity nitrogen and a small amount of liquid oxygen, liquid nitrogen simultaneously, product oxygen pressure 2 ~ 3.5bar, nitrogen pressure 5 ~ 10bar.
For this industry air separation unit, if adopt pressure-variable adsorption, need to arrange three cover pressure-swing absorption apparatus, energy consumption is high, less economical, can not produce liquid, and production by pressure swing adsorption high purity oxygen difficulty is large, should not be used for large-scale industry gas; If adopt two cover cryogenic air separation unit devices, investment is large, floor space is large, and science is not unreasonable.
The raw material of air separation unit is air, and its main consumption is the energy, and therefore, how further, reduction energy ezpenditure seems particularly important.The product of air separation unit is oxygen, and security is also very important, provides more low energy consumption more reasonably technological process, not only can accomplish to reduce energy consumption, reduce production cost, improve overall economic benefit, for society economizes on resources, the social environment of establishment low-carbon (LC), environmental protection plays a role.
For metallurgy type air separation unit, both can adopt external compression flow process, also can adopt Internal-compression flow, adopt which kind of Process flow actually, according to the product demand of user, should consider from energy consumption, investment, operation, the several aspect of security.Internal-compression flow increases than external compression flow process heat exchange irreversible loss, and in this sense, pressure energy consumption wants high, but the compressor of air separation unit is large electricity consumer, and the energy consumption of efficiency to whole device of compressor plays a part very important.For the nonferrous smelting air separation unit that oxygen pressure is not high, the saturating efficiency of the domestic oxygen of external compression flow process is low, and energy consumption is high, and the saturating security of oxygen is poor, and Operation and Maintenance amount is large; And adopt Internal-compression flow supercharger one stage of compression, adopt import, efficiency is high, and energy consumption is low, and interior pressure security is good.
Current variable-pressure adsorption equipment only produces single product, can only obtain low-purity oxygen product, or adopts purification method to obtain high purity oxygen again, and can not produce fluid product.Adopt two cover air separation units to produce low purity oxygen, high purity oxygen respectively, investment is large, energy consumption is high, and science is not unreasonable.
Utility model content
The purpose of this utility model is to overcome the shortcoming existed in above-mentioned prior art provides a kind of oxygen product, energy consumption simultaneously obtaining different purity low and the cryogenic separation that economy security is good and produce the device of low purity oxygen, high purity oxygen and nitrogen.
The good effect that the technical solution of the utility model produces is as follows: the device of a kind of cryogenic separation and production low purity oxygen, high purity oxygen and nitrogen, comprise air compression system, front end precooling purification system and ice chest, described air compression system comprises air compressor machine and air booster, described ice chest comprises main heat exchanger, liquid oxygen evaporator, liquid oxygen pump, the expanding end of decompressor and rectifying column, and described rectifying column comprises Xia Ta, Shang Ta, pure oxygen tower, pure oxygen tower evaporimeter and the main condenser evaporimeter between Shang Ta and lower tower; Described air compressor machine is connected with front end precooling purification system by the first pipeline, and the gas vent of described front end precooling purification system is connected with described lower tower through main heat exchanger by second pipe; The gas vent of described front end precooling purification system is connected with the pressurized end of a decompressor by the 3rd pipeline, described pressurized end connects a water cooler by the 4th pipeline, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline; The gas vent of described front end precooling purification system is connected with described air booster by the 6th pipeline, the outlet of air booster final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 7th pipeline, and post liquefaction is by entering in the middle part of described lower tower after the 8th pipeline and first throttle valve; Described expanding end outlet arranges the 9th pipeline and is connected with upper tower; Described lower tower bottom liquid outlet is connected in the middle part of described upper tower after a subcooler is by the tenth pipeline and second throttle; Described lower tower central liquid exit is connected in the middle part of described upper tower after a subcooler is by the 11 pipeline and the 3rd choke valve; The liquid outlet of described lower top of tower is connected to described upper top of tower by the 12 pipeline after described subcooler and the 4th choke valve; The gas vent of described lower top of tower is connected on described pure oxygen tower evaporimeter by the 13 pipeline, and the liquid outlet of described pure oxygen tower evaporimeter is connected to described upper top of tower by the 14 pipeline and the 5th choke valve; The gas vent of described lower top of tower is connected to ice chest outside as product pressure nitrogen by the 15 pipeline after main heat exchanger; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected to described pure oxygen top of tower by the 16 pipeline; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected with described liquid oxygen pump by the 17 pipeline, liquid oxygen pump outlet is connected with described liquid oxygen evaporator by the 18 pipeline, and the gas oxygen of described liquid oxygen evaporator is sent as product by the 19 pipeline cooling box after main heat exchanger re-heat; The dirty nitrogen outlet place of described upper top of tower connects the 20 pipeline, and described 20 pipeline is connected to the purification system of ice chest outside after described subcooler and main heat exchanger; Described pure oxygen top of tower gas vent is connected with described upper tower bottom by the 21 pipeline; Described pure oxygen tower bottom liquid oxygen is connected with described liquid oxygen pump by the 22 pipeline, liquid oxygen pump outlet is connected with described liquid oxygen evaporator by the 23 pipeline, and the gas oxygen of described liquid oxygen evaporator is sent as product by the 24 pipeline cooling box after main heat exchanger re-heat.
Described lower tower operating pressure 0.38MPa.
Described lower tower to be the number of plates be 25 ~ 40 or corresponding tower tray number be the lower towers of 35 ~ 60 dishes, described upper tower to be the number of plates be 30 ~ 40 or corresponding tower tray number be 52 ~ 68 dishes structured packings on tower, described pure oxygen tower to be the number of plates be 20 ~ 30 or corresponding tower tray number be the regular packed towers of 35 ~ 52 dishes.
Cryogenic separation and produce being separated and a production method of device of low purity oxygen, high purity oxygen and nitrogen, the method is as follows:
Go out the air after purifying and be divided into three parts: Part I air enters main heat exchanger, the gas that backflowed cooling laggard enter lower tower; The air that Part II is equivalent to swell increment enters the pressurized end supercharging of turbo-expander, through (after supercharging) cooler cooling laggard enter main heat exchanger, extract out in the middle part of main heat exchanger after being cooled to uniform temperature and enter decompressor, the air after expansion sends into upper tower; Part III air enters air booster and compresses further, after main heat exchanger cooling, enter liquid oxygen evaporator as thermal source liquid oxygen vaporisation, go out liquid oxygen evaporator laggard enter in the middle part of lower tower;
Lower tower produces following product from top to bottom: liquid nitrogen, lean solution sky and oxygen-enriched liquid air; Described oxygen-enriched liquid air throttling enters Shang Ta, as its phegma; Lean solution sky is crossed cold deutomerite through subcooler and is flow to into upper tower, as its phegma; Liquid nitrogen divides three parts: a part is crossed top of tower in cold rear feeding and made phegma in subcooler, a part is as lower tower phegma, part liquid nitrogen is compressed into required pressure in liquid nitrogen pump, then delivers in heat exchanger and obtains pressure nitrogen gas by carrying out heat exchange with air.
Upper tower produces following product from top to bottom and comprises: top produces dirty nitrogen, bottom produces rich solution oxygen and Shang Ta; Dirty nitrogen extract out from upper top of tower after through subcooler and main heat exchanger re-heat to design temperature cooling box, one dirty nitrogen is used for the regeneration of molecular sieve adsorber, another strand of dirty nitrogen is delivered to water-cooling tower and is cooled water, also has sub-fraction to enter ice chest, inflates ice chest; Rich solution oxygen is extracted out from upper tower bottom, is compressed into required pressure, then enters liquid oxygen evaporator in liquid oxygen pump, is heated by the air that vaporization is laggard to be entered to be sent to user after main heat exchanger re-heat to normal temperature; Deliver to the rectifying of pure oxygen tower from upper tower bottom extraction section rich solution oxygen and obtain liquid oxygen.
The rich solution oxygen come from upper tower bottom enters pure oxygen top of tower, and obtain more than 99.6% pure liquid oxygen in bottom after rectifying, top crude oxygen returns tower; After the pure liquid oxygen of pure oxygen tower bottom sends into main heat exchanger re-heat after liquid oxygen pump pressurization, cooling box obtains oxygen.
The gas of decompressor pressurized end is from the gas after low-pressure air compressor machine.
High-purity nitrogen can be obtained from Xia Ta, nitrogen pressure nitrogen pressure 0.35MPa, or adopt pressure in liquid nitrogen pump to obtain the higher nitrogen of pressure from lower top of tower extraction liquid nitrogen.
The good effect that the technical solution of the utility model produces is as follows: obtain low purity oxygen, high purity oxygen, high-purity nitrogen, low-purity liquid oxygen, high-purity liquid oxygen, liquid nitrogen product simultaneously, compression in oxygen adopts, save oxygen compressor, security is good, be specially adapted to the supporting sky of nonferrous smelting divide, the low-purity oxygen product purity 90% ~ 95% obtained, high-purity oxygen product purity >=99.6%, nitrogen gas purity >=99.9%.
A set of air separation unit obtains multiple product simultaneously, solves the problem that many covering devices could realize, and not only can accomplish to reduce energy consumption, reduces production cost, can also save human resources, reduce investment outlay, scientific and reasonable.This utility model is significant to increasing economic efficiency, and to saving social resources, the social environment of establishment low-carbon (LC), environmental protection plays a positive role.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model cryogenic separation and the device producing low purity oxygen, high purity oxygen and nitrogen.
Be labeled as in figure: 1, air compressor machine; 2, front end precooling purification system; 3, air booster; 4, turbo-expander pressurized end; 5, water cooler; 6, main heat exchanger; 7, the first liquid oxygen evaporator; 8, Xia Ta; 9, main condenser evaporimeter; 10, Shang Ta; 11, subcooler; 12, pure oxygen tower; 13, pure oxygen tower evaporimeter; 14, turbo-expander expanding end; 15, the second liquid oxygen evaporator; 16, the first liquid oxygen pump; 17, the second liquid oxygen pump; 18, first throttle valve; 19, second throttle; 20, the 3rd choke valve; 21, the 4th choke valve; 22, the 5th choke valve; 23, ice chest; 101, the first pipeline; 102, second pipe; 103, the 3rd pipeline; 104, the 4th pipeline; 105, the 5th pipeline; 106, the 6th pipeline; 107, the 7th pipeline; 108, the 8th pipeline; 109, the 9th pipeline; 110, the tenth pipeline; 111, the 11 pipeline; 112, the 12 pipeline; 113, the 13 pipeline; 114, the 14 pipeline; 115, the 15 pipeline; 116, the 16 pipeline; 117, the 17 pipeline; 118, the 18 pipeline; 119, the 19 pipeline; 120, the 20 pipeline; 121, the 21 pipeline; 122, the 22 pipeline; 123, the 23 pipeline; 124, the 24 pipeline.
Detailed description of the invention
Embodiment one
The device of cryogenic separation and production low purity oxygen, high purity oxygen and nitrogen, as shown in Figure 1, comprise air compression system, front end precooling purification system 2 and ice chest 24, described air compression system comprises air compressor machine 1, air booster 3, described ice chest comprises main heat exchanger 6, first liquid oxygen evaporator 7, second liquid oxygen evaporator 15, first liquid oxygen pump 16, second liquid oxygen pump 17, turbo-expander expanding end 14 and rectifying column, and described rectifying column comprises lower tower 8, upper tower 10, pure oxygen tower 12, pure oxygen tower evaporimeter 13 and the main condenser evaporimeter 9 between Shang Ta and lower tower.Described air compressor machine is connected with front end precooling purification system by the first pipeline 101, and the gas vent of described front end precooling purification system is connected with described lower tower through main heat exchanger by second pipe 102; The gas vent of described front end precooling purification system is connected with a turbo-expander pressurized end 4 by the 3rd pipeline 103, described pressurized end connects a water cooler 5 by the 4th pipeline 104, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline 105; The gas vent of described front end precooling purification system is connected with described air booster by the 6th pipeline 106, the outlet of air booster final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 7th pipeline 107, and post liquefaction is by entering in the middle part of described lower tower after the 8th pipeline 108 and first throttle valve 18; Described expanding end outlet arranges the 9th pipeline 109 and is connected with upper tower; Described lower tower bottom liquid outlet is connected in the middle part of described upper tower after a subcooler is by the tenth pipeline 110 and second throttle 19; Described lower tower central liquid exit is connected in the middle part of described upper tower after a subcooler 11 is by the 11 pipeline 111 and the 3rd choke valve 20; The liquid outlet of described lower top of tower is connected to described upper top of tower by the 12 pipeline 112 after described subcooler and the 4th choke valve 21; The gas vent of described lower top of tower is connected to the evaporation of described pure oxygen tower by the 13 pipeline 113, and gas goes out after evaporator condensation becomes liquid, by being connected to described upper top of tower after the 14 pipeline 114 and the 5th choke valve 22; The gas vent of described lower top of tower is connected to ice chest outside as product pressure nitrogen by the 15 pipeline 115 after main heat exchanger; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected to described pure oxygen top of tower by the 16 pipeline 116; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected with described first liquid oxygen pump by the 17 pipeline 117, first liquid oxygen pump outlet is connected with described first liquid oxygen evaporator by the 18 pipeline 118, and the gas oxygen of described first liquid oxygen evaporator is sent as product by the 19 pipeline 119 cooling box after main heat exchanger re-heat.The dirty nitrogen outlet place of described upper top of tower connects the 20 pipeline 120, and described 20 pipeline is connected to the purification system of ice chest outside after described subcooler and main heat exchanger.Described pure oxygen top of tower gas is connected with described upper tower bottom by the 21 pipeline 121; Described pure oxygen tower bottom liquid oxygen is connected with described second liquid oxygen pump by the 22 pipeline 122, second liquid oxygen pump outlet is connected with described second liquid oxygen evaporator by the 23 pipeline 123, and the gas oxygen of described second liquid oxygen evaporator is sent as product by the 24 pipeline 124 cooling box after main heat exchanger re-heat.
embodiment two
A device and method for cryogenic separation and production low purity oxygen, high purity oxygen and nitrogen, the method is as follows:
Go out the air after purifying and be divided into three parts: Part I air enters main heat exchanger, the gas that backflowed cooling laggard enter lower tower; The air that Part II is equivalent to swell increment enters the pressurized end supercharging of turbo-expander, through (after supercharging) cooler cooling laggard enter main heat exchanger, extract out in the middle part of main heat exchanger after being cooled to uniform temperature and enter decompressor, the air after expansion sends into upper tower; Part III air enters air booster and compresses further, after main heat exchanger cooling, enter liquid oxygen evaporator as thermal source liquid oxygen vaporisation, go out liquid oxygen evaporator laggard enter in the middle part of lower tower;
Lower tower produces following product from top to bottom: liquid nitrogen, lean solution sky and oxygen-enriched liquid air; Described oxygen-enriched liquid air throttling enters Shang Ta, as its phegma; Lean solution sky is crossed cold deutomerite through subcooler and is flow to into upper tower, as its phegma; Liquid nitrogen divides three parts: a part is crossed top of tower in cold rear feeding and made phegma in subcooler, a part is as lower tower phegma, part liquid nitrogen is compressed into required pressure in liquid nitrogen pump, then delivers in heat exchanger and obtains pressure nitrogen gas by carrying out heat exchange with air.
Upper tower produces following product from top to bottom and comprises: top produces dirty nitrogen, bottom produces rich solution oxygen and Shang Ta; Dirty nitrogen extract out from upper top of tower after through subcooler and main heat exchanger re-heat to design temperature cooling box, one dirty nitrogen is used for the regeneration of molecular sieve adsorber, another strand of dirty nitrogen is delivered to water-cooling tower and is cooled water, also has sub-fraction to enter ice chest, inflates ice chest; Rich solution oxygen is extracted out from upper tower bottom, is compressed into required pressure, then enters liquid oxygen evaporator in liquid oxygen pump, is heated by the air that vaporization is laggard to be entered to be sent to user after main heat exchanger re-heat to normal temperature; Deliver to the rectifying of pure oxygen tower from upper tower bottom extraction section rich solution oxygen and obtain liquid oxygen.
The rich solution oxygen come from upper tower bottom enters pure oxygen top of tower, and obtain more than 99.6% pure liquid oxygen in bottom after rectifying, top crude oxygen returns tower; After the pure liquid oxygen of pure oxygen tower bottom sends into main heat exchanger re-heat after liquid oxygen pump pressurization, cooling box obtains oxygen.
The gas of decompressor pressurized end is from the gas after low-pressure air compressor machine.
High-purity nitrogen can be obtained from Xia Ta, nitrogen pressure 0.35MPa, or adopt pressure in liquid nitrogen pump to obtain the higher nitrogen of pressure from lower top of tower extraction liquid nitrogen.
Claims (3)
1. the device of a cryogenic separation and production low purity oxygen, high purity oxygen and nitrogen, comprise air compression system, front end precooling purification system and ice chest, described air compression system comprises air compressor machine and air booster, described ice chest comprises main heat exchanger, liquid oxygen evaporator, liquid oxygen pump, the expanding end of decompressor and rectifying column, and described rectifying column comprises Xia Ta, Shang Ta, pure oxygen tower, pure oxygen tower evaporimeter and the main condenser evaporimeter between Shang Ta and lower tower; It is characterized in that: described air compressor machine is connected with front end precooling purification system by the first pipeline, the gas vent of described front end precooling purification system is connected with described lower tower through main heat exchanger by second pipe; The gas vent of described front end precooling purification system is connected with the pressurized end of a decompressor by the 3rd pipeline, described pressurized end connects a water cooler by the 4th pipeline, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline; The gas vent of described front end precooling purification system is connected with described air booster by the 6th pipeline, the outlet of air booster final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 7th pipeline, and post liquefaction is by entering in the middle part of described lower tower after the 8th pipeline and first throttle valve; Described expanding end outlet arranges the 9th pipeline and is connected with upper tower; Described lower tower bottom liquid outlet is connected in the middle part of described upper tower after a subcooler is by the tenth pipeline and second throttle; Described lower tower central liquid exit is connected in the middle part of described upper tower after a subcooler is by the 11 pipeline and the 3rd choke valve; The liquid outlet of described lower top of tower is connected to described upper top of tower by the 12 pipeline after described subcooler and the 4th choke valve; The gas vent of described lower top of tower is connected on described pure oxygen tower evaporimeter by the 13 pipeline, and the liquid outlet of described pure oxygen tower evaporimeter is connected to described upper top of tower by the 14 pipeline and the 5th choke valve; The gas vent of described lower top of tower is connected to ice chest outside as product pressure nitrogen by the 15 pipeline after main heat exchanger; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected to described pure oxygen top of tower by the 16 pipeline; The low pure liquid oxygen side outlet place of described main condenser evaporimeter is connected with described liquid oxygen pump by the 17 pipeline, liquid oxygen pump outlet is connected with described liquid oxygen evaporator by the 18 pipeline, and the gas oxygen of described liquid oxygen evaporator is sent as product by the 19 pipeline cooling box after main heat exchanger re-heat; The dirty nitrogen outlet place of described upper top of tower connects the 20 pipeline, and described 20 pipeline is connected to the purification system of ice chest outside after described subcooler and main heat exchanger; Described pure oxygen top of tower gas vent is connected with described upper tower bottom by the 21 pipeline; Described pure oxygen tower bottom liquid oxygen is connected with described liquid oxygen pump by the 22 pipeline, liquid oxygen pump outlet is connected with described liquid oxygen evaporator by the 23 pipeline, and the gas oxygen of described liquid oxygen evaporator is sent as product by the 24 pipeline cooling box after main heat exchanger re-heat.
2. the device of cryogenic separation according to claim 1 and production low purity oxygen, high purity oxygen and nitrogen, is characterized in that: described lower tower operating pressure 0.38MPa.
3. the device of cryogenic separation according to claim 1 and production low purity oxygen, high purity oxygen and nitrogen, it is characterized in that: described lower tower to be the number of plates be 25 ~ 40 or corresponding tower tray number be the lower towers of 35 ~ 60 dishes, described upper tower to be the number of plates be 30 ~ 40 or corresponding tower tray number be 52 ~ 68 dishes structured packings on tower, described pure oxygen tower to be the number of plates be 20 ~ 30 or corresponding tower tray number be the regular packed towers of 35 ~ 52 dishes.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520715331.3U CN205079543U (en) | 2015-09-16 | 2015-09-16 | Device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520715331.3U CN205079543U (en) | 2015-09-16 | 2015-09-16 | Device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen |
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| CN205079543U true CN205079543U (en) | 2016-03-09 |
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| CN201520715331.3U Expired - Fee Related CN205079543U (en) | 2015-09-16 | 2015-09-16 | Device of cryogenic separation and production low -purity oxygen, high purity oxygen and nitrogen |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105066587A (en) * | 2015-09-16 | 2015-11-18 | 开封空分集团有限公司 | Cryogenic separation and low-purity oxygen and high-purity oxygen and nitrogen production device and method |
| CN112066644A (en) * | 2020-09-18 | 2020-12-11 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for producing high-purity nitrogen and low-purity oxygen |
-
2015
- 2015-09-16 CN CN201520715331.3U patent/CN205079543U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105066587A (en) * | 2015-09-16 | 2015-11-18 | 开封空分集团有限公司 | Cryogenic separation and low-purity oxygen and high-purity oxygen and nitrogen production device and method |
| CN112066644A (en) * | 2020-09-18 | 2020-12-11 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for producing high-purity nitrogen and low-purity oxygen |
| US11988446B2 (en) | 2020-09-18 | 2024-05-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for producing high-purity nitrogen and low-purity oxygen |
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
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Granted publication date: 20160309 Termination date: 20180916 |