WO2016084754A1 - アンモニア処理システム - Google Patents
アンモニア処理システム Download PDFInfo
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- WO2016084754A1 WO2016084754A1 PCT/JP2015/082777 JP2015082777W WO2016084754A1 WO 2016084754 A1 WO2016084754 A1 WO 2016084754A1 JP 2015082777 W JP2015082777 W JP 2015082777W WO 2016084754 A1 WO2016084754 A1 WO 2016084754A1
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- boiler
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines
Definitions
- the present invention relates to an ammonia treatment system, and more particularly, to an ammonia treatment system for treating ammonia contained in boiler wastewater that is wastewater from boiler equipment.
- This application claims priority about Japanese Patent Application No. 2014-238737 for which it applied on November 26, 2014, and uses the content here.
- hydrazine is used to remove oxygen that causes corrosion. Since hydrazine is regarded as a “chemical substance with recognized mutagenicity”, the adoption of safer oxygen scavengers and water treatment without oxygen scavengers has been progressing in recent years.
- an oxygen scavenger that does not use hydrazine ammonia having a high hydrogen ion exponent (pH) (for example, pH 7 to pH 10.5) is known.
- PH hydrogen ion exponent
- reduction of nitrogen is also required by the drainage regulations, and an immediate response is desired.
- Patent Document 1 describes an ammonia treatment system that decomposes ammonia by chlorination using sodium hypochlorite (sodium hypochlorite) obtained by electrolyzing seawater.
- sodium hypochlorite sodium hypochlorite
- the capacity of the mixing tank is determined according to the reaction time of boiler wastewater and hypochlorous acid.
- the reaction time between the boiler wastewater and hypochlorous acid becomes long, it is necessary to increase the capacity of the mixing tank.
- An object of the present invention is to provide an ammonia treatment system that can shorten the reaction time between boiler wastewater and hypochlorous acid.
- the ammonia treatment system includes a drainage line for supplying boiler wastewater to the mixing tank, a pH measuring device for measuring the pH of the boiler wastewater flowing through the drainage line, and the drainage line. And a pH adjusting device for adding a pH adjusting agent for adjusting the pH of the boiler wastewater to the boiler wastewater, and an electrolytic device for electrolyzing seawater or salt water to generate electrolytically treated water having hypochlorous acid. Based on the measured value of the pH measuring device, a supply line that is provided upstream from the junction of the drainage line and the mixing tank and that supplies hypochlorous acid generated by the electrolysis device to the boiler drainage And a control device for controlling the amount of the pH adjuster added.
- the reaction time between the boiler wastewater and hypochlorous acid can be shortened by adding a pH adjuster to adjust the pH of the boiler wastewater.
- the pH measuring device is disposed downstream of the pH adjusting device and at a position where the pH of the boiler wastewater adjusted by the pH adjusting agent added by the pH adjusting device is stable. May be.
- the pH of the boiler wastewater can be measured more accurately by the pH measuring device.
- adjustment of pH of boiler drainage by a pH adjustment device can be performed correctly.
- the ammonia treatment system includes a storage tank that is provided upstream of the drainage line and stores the boiler drainage, and a storage tank pH measurement device that measures the pH of the boiler drainage stored in the storage tank.
- the said control apparatus may control the amount of hypochlorous acid produced
- the reaction time between boiler wastewater and hypochlorous acid can be shortened by adding a pH adjuster to adjust the pH of the boiler wastewater.
- FIG. 1 is a schematic configuration diagram of a plant P having an ammonia treatment system 1 according to the first embodiment of the present invention.
- the ammonia treatment system 1 is a system for treating boiler waste water W discharged from a combined cycle power plant P having an exhaust heat recovery boiler B.
- the ammonia treatment system 1 includes a seawater electrolysis device 2 and a control device 8 as main components.
- a combined cycle power plant P (hereinafter referred to as plant P) includes a gas turbine (not shown), an exhaust heat recovery boiler B (hereinafter referred to as boiler B) to which exhaust gas from the gas turbine is sent, and a steam turbine. (Not shown) and a generator (not shown) that generates electric power by being driven by the rotational driving force of the gas turbine and the steam turbine.
- Seawater M taken from the seawater intake 3 through the first seawater supply line 4 is introduced into the plant P. Seawater M is used for applications such as cooling.
- the first seawater supply line 4 is provided with a seawater supply pump (not shown) that supplies the seawater M and a seawater flow rate adjustment valve (not shown) that adjusts the flow rate of the seawater M.
- a seawater supply pump (not shown) that supplies the seawater M
- a seawater flow rate adjustment valve (not shown) that adjusts the flow rate of the seawater M.
- ammonia is used as an oxygen scavenger for removing oxygen that causes corrosion. Therefore, the boiler waste water W discharged from the boiler B is an ammonia nitrogen-containing waste water containing ammonia nitrogen such as ammonia (NH 3 ) and ammonium ions (NH 4 + ).
- the boiler waste water W discharged from the boiler B is stored in the storage tank 5.
- the storage tank 5 is provided with a dilution water introducing device 6 for introducing a temperature-reduced diluted water (industrial water supply) for reducing the temperature of the boiler waste water W into the storage tank 5.
- the treated water in the storage tank 5 is managed below a predetermined temperature based on the temperature measured by a thermometer (not shown) that can measure the temperature of the treated water.
- the storage tank 5 is provided with a storage tank pH measurement device 7 that measures the pH (hydrogen ion index) of the treated water in the storage tank 5.
- a mixing tank 9 is provided on the downstream side of the storage tank 5.
- the storage tank 5 and the mixing tank 9 are connected via a drainage line 10.
- the boiler waste water W stored in the storage tank 5 and reduced in temperature is introduced into the mixing tank 9 through the drain line 10.
- the boiler waste water W is discharged after being introduced into the mixing tank 9.
- the drainage line 10 is provided with a drainage supply pump 16 that feeds the boiler drainage W stored in the storage tank 5 to the mixing tank 9.
- the seawater electrolysis apparatus 2 is an apparatus that performs electrolysis of the seawater M introduced from the water intake 3 through the second seawater supply line 11.
- the second seawater supply line 11 is provided with a seawater supply pump 14 that supplies the seawater M and a seawater flow rate adjustment valve 15 that adjusts the flow rate of the seawater M.
- the seawater electrolysis apparatus 2 includes an electrolytic cell 12 and a DC power supply device 13.
- the seawater electrolysis apparatus 2 is an apparatus that generates electrolyzed water E containing sodium hypochlorite (chlorine, sodium hypochlorite) by electrolyzing seawater M.
- the electrolytic cell 12 has a plurality of electrodes (not shown).
- the DC power supply device 13 is a device that supplies a current to be used for electrolysis of seawater M.
- the DC power supply device 13 for example, a configuration including a DC power supply and a constant current control circuit can be employed.
- the DC power source is a power source that outputs DC power.
- the DC power supply may be configured to rectify and output AC power output from the AC power supply to DC, for example.
- the seawater electrolysis apparatus 2 of the present embodiment is a one-through system in which the seawater M is passed through the electrolytic cell 12 only once.
- a recycling method for circulating seawater may be adopted.
- the downstream side of the electrolytic cell 12 (outlet of the electrolytic cell 12) and the upstream side of the electrolytic cell 12 (inlet of the electrolytic cell 12) are connected by a circulation channel to circulate seawater.
- the seawater electrolysis device 2 may be of any type as long as it can generate hypochlorous acid using the seawater M.
- the electrolyzed water E generated in the seawater electrolyzer 2 is introduced into the mixing tank 9 via the supply line 18 and mixed with the boiler waste water W.
- a line mixer 21 that promotes mixing of the boiler wastewater W and the electrolytically treated water E is provided on the drainage line 10 and on the downstream side (mixing tank 9 side) of the junction 20 with the supply line 18. Yes.
- Boiler waste water W and electrolytically treated water E are introduced into the mixing tank 9, and ammonia and hypochlorous acid present in the boiler waste water W undergo a solution reaction and are decomposed to nitrogen gas (N 2 ). That is, in the mixing tank 9, ammonia is processed and the boiler waste water W is in a state where it can be discharged.
- a pH adjusting device 23 that adjusts the pH (hydrogen ion index) of the boiler drainage W that flows through the drainage line 10 in order from the upstream side, and a pH measurement device that measures the pH of the boiler drainage W. 24 is provided.
- the pH adjusting device 23 and the pH measuring device 24 are provided on the upstream side of the junction 20 of the drain line 10 and the supply line 18. That is, the pH measuring device 24 is provided on the downstream side of the pH adjusting device 23, and the electrolytically treated water E is mixed on the downstream side of the pH measuring device 24.
- the pH adjusting device 23 is a device that adjusts the pH of the boiler drainage W by adding a pH adjuster to the boiler drainage W flowing through the drainage line 10.
- An acid or alkali agent such as hydrochloric acid is used as the pH adjuster.
- the boiler waste water W of the present embodiment is often on the alkaline side, and hydrochloric acid is mainly added.
- the pH measuring device 24 is installed sufficiently downstream of the pH adjusting device 23. Specifically, the pH measuring device 24 is arranged at a position where the pH adjusting agent added by the pH adjusting device 23 can be mixed with the boiler waste water W and can measure the pH of the boiler waste water W after reacting appropriately. . In other words, the pH measuring device 24 is disposed at a position where the pH of the boiler waste water W adjusted by the pH adjusting agent added by the pH adjusting device 23 is stabilized.
- the pH adjusting device 23 is controlled to adjust the addition amount of the pH adjusting agent.
- the control device 8 controls the pH adjusting device 23 so that hydrochloric acid is added to the boiler waste water W.
- the boiler waste water W discharged from the boiler B is stored in the storage tank 5.
- the pH of the boiler waste water W of this embodiment is around 10.5, indicating alkalinity.
- the temperature-reduced diluted water is introduced into the storage tank 5.
- the pH of the boiler waste water W in the storage tank 5 becomes 9.9, for example.
- the boiler waste water W stored in the storage tank 5 is fed to the drain line 10 at a predetermined speed using the drain supply pump 16.
- the control device 8 inputs a pH adjusting agent into the boiler waste water W using the pH adjusting device 23 based on the pH measured by the pH measuring device 24.
- the control device 8 controls the pH adjusting device 23 so that the pH of the boiler waste water W becomes 7.5 to 9.5.
- control device 8 calculates the required amount of hypochlorous acid based on the pH of the boiler waste water W measured by the storage tank pH measurement device 7 and determines the output current value of the DC power supply device 13. And the amount E of electrolytic treatment water required from the processing time etc. in the mixing tank 9 is determined.
- the nitrogen concentration in the storage tank 5 is known by measuring the pH of the boiler waste water W.
- the amount of hypochlorous acid with respect to the ammoniacal nitrogen concentration is also correlated, and the amount of hypochlorous acid increases or decreases in proportion to the current value of the DC power supply device 13. Therefore, it is possible to control the DC power supply 13 by measuring the pH of the boiler waste water W in the storage tank 5 and determine the amount of hypochlorous acid produced (ammonia nitrogen removal amount).
- the ammonia contained in the boiler waste water W can be decomposed
- reaction time between the boiler waste water W and hypochlorous acid can be shortened by adding a pH adjuster to adjust the pH of the boiler waste water W.
- reaction time between the boiler waste water W and hypochlorous acid can be further shortened by adjusting the pH to the range of 7.5 to 9.5.
- the pH adjuster added to the boiler waste water W is added on the upstream side of the merging portion 20 to which the electrolytically treated water E is supplied, so that it is not affected by the pH fluctuation caused by the electrolytically treated water E.
- the pH of the boiler waste water W can be adjusted.
- the ammonia treatment system 1 ⁇ / b> B of the present embodiment has an injection line 17 that injects the electrolytically treated water E generated by the seawater electrolysis apparatus 2 into the water inlet 3.
- the electrolyzed water E sodium hypochlorite
- the seawater electrolysis apparatus 2 of this embodiment has a function as a marine organism adhesion prevention apparatus.
- a supply line 18 for supplying electrolytically treated water E to the mixing tank 9 is branched from an injection line 17 that connects the seawater electrolyzer 2 and the water intake 3. That is, the electrolytically treated water E generated by the seawater electrolyzer 2 is introduced into the mixing tank 9 through the supply line 18 branched from the injection line 17 and mixed with the boiler waste water W.
- the supply line 18 is provided with a flow rate adjusting valve 19 that adjusts the flow rate of the electrolytically treated water E.
- the control device 8 controls the amount of electrolytically treated water E (sodium hypochlorite) injected from the injection line 17 by adjusting the flow rate adjusting valve 19. Similar to the control device 8 of the first embodiment, the control device 8 calculates the required amount of hypochlorous acid based on the pH of the boiler waste water W measured by the storage tank pH measurement device 7, and the DC power supply device 13. Determine the output current value. And the amount E of electrolytic treatment water required from the processing time etc. in the mixing tank 9 is determined.
- E sodium hypochlorite
- the electrolytically treated water E generated by the seawater electrolysis apparatus 2 is injected into the intake 3 of the seawater M through the injection line 17.
- the electrolyzed water E By injecting the electrolyzed water E into the water intake 3, adhesion of marine organisms to the water intake 3 can be suppressed.
- the supply line 18 of the electrolytically treated water E according to the above embodiment is connected to the drainage line 10 through which the boiler drainage W flows, but the supply line 18 may be directly connected to the mixing tank 9.
- the configuration in which the seawater M is introduced into the seawater electrolysis apparatus 2 is described, but the configuration in which saltwater is introduced into the seawater electrolysis apparatus 2 may be employed. That is, the liquid introduced into the seawater electrolysis apparatus 2 only needs to contain chlorine ions (Cl ⁇ ) like the seawater M.
- a means for measuring pH, residual chlorine, water quality, etc. may be provided downstream of the mixing tank 9 or the mixing tank 9, and a line for returning the waste water to the storage tank 5 when the waste water does not meet the standard may be provided.
- the reaction time between boiler wastewater and hypochlorous acid can be shortened by adding a pH adjuster to adjust the pH of the boiler wastewater.
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Abstract
Description
本願は、2014年11月26日に出願された特願2014-238637号について優先権を主張し、その内容をここに援用する。
ヒドラジンを用いない脱酸素剤としては、水素イオン指数(pH)の値を大きくした(例えばpH7~pH10.5)アンモニアが知られている。しかしながら、脱酸素剤としてアンモニアを用いることにより今後プラントからの排水のアンモニア濃度が高くなることが想定されている(例えば非特許文献1参照)。一方、排水規制により窒素の低減も求められており、早急な対応が望まれている。
以下、本発明の第一実施形態のアンモニア処理システム1について図面を参照して詳細に説明する。
図1は、本発明の第一実施形態のアンモニア処理システム1を有するプラントPの概略構成図である。図1に示すように、アンモニア処理システム1は、排熱回収ボイラBを備えたコンバインドサイクル発電プラントPから排出されるボイラ排水Wを処理するためのシステムである。
コンバインドサイクル発電プラントP(以下、プラントPと呼ぶ)は、ガスタービン(図示せず)と、ガスタービンからの排気ガスが送られる排熱回収ボイラB(以下、ボイラBと呼ぶ)と、蒸気タービン(図示せず)と、ガスタービンと蒸気タービンの回転駆動力により駆動されて発電する発電機(図示せず)と、を有する構成とすることができる。
例えばボイラBのボイラ水には、腐食の要因となる酸素を除去するための脱酸素剤としてアンモニアが使用されている。よって、ボイラBから排出されるボイラ排水Wは、アンモニア(NH3)、アンモニウムイオン(NH4 +)等のアンモニア性窒素を含むアンモニア性窒素含有排水である。
海水電解装置2は、電解槽12と、直流電源装置13と、を有している。海水電解装置2は、海水Mを電気分解することによって、次亜塩素酸ナトリウム(塩素、次亜塩素酸ソーダ)を含む電解処理水Eを生成する装置である。電解槽12は、複数の電極(図示せず)を有している。
排水ライン10上であって、供給ライン18との合流部20よりも下流側(混合槽9側)には、ボイラ排水Wと電解処理水Eとの混合を促進するラインミキサ21が設けられている。
この関係に基づき、制御装置8は、pH測定装置24の測定値、即ち排水ライン10の合流部20よりも上流側のボイラ排水WのpHがpH=7.5~9.5となるように、pH調整装置23を制御してpH調整剤の添加量を調整する。例えば、制御装置8は、ボイラ排水WのpHが10(アルカリ側)であった場合、ボイラ排水Wに塩酸を添加するようにpH調整装置23を制御する。
まず、ボイラBから排出されたボイラ排水Wは、貯留槽5に貯留される。本実施形態のボイラ排水WのpHは、10.5前後であり、アルカリ性を示している。ボイラ排水Wと同時に、減温希釈水が貯留槽5に投入される。これにより、貯留槽5内のボイラ排水WのpHは例えば9.9となる。貯留槽5に貯留されたボイラ排水Wは、排水供給ポンプ16を用いて所定速度で排水ライン10に送水される。
また、貯留槽5内のボイラ排水WのpHを測定することによって、直流電源装置13を制御し、次亜塩素酸の生成量を決定することが可能となる。
以下、本発明の第二実施形態のアンモニア処理システム1Bを図面に基づいて説明する。なお、本実施形態では、上述した第一実施形態との相違点を中心に述べ、同様の部分についてはその説明を省略する。
例えば、上記実施形態の電解処理水Eの供給ライン18は、ボイラ排水Wが流れる排水ライン10に接続されているが、供給ライン18を直接混合槽9に接続してもよい。
例えば、上記実施形態では、海水電解装置2には海水Mが導入される構成を示したが、海水電解装置2に塩水を導入する構成としてもよい。即ち、海水電解装置2に導入される液体は、海水Mと同様に塩素イオン(Cl-)を含んでいればよい。
また、混合槽9又は混合槽9の下流にpH、残留塩素、水質などを測定する手段を設けて、廃水が基準に満たない場合に、廃水を貯留槽5に戻すラインを設けてもよい。
2 海水電解装置(電解装置)
3 取水口
4 第一海水供給ライン
5 貯留槽
6 希釈水導入装置
7 貯留槽pH測定装置
8 制御装置
9 混合槽
10 排水ライン
11 第二海水供給ライン
12 電解槽
13 直流電源装置
14 海水供給ポンプ
15 海水流量調整バルブ
16 排水供給ポンプ
17 注入ライン
18 供給ライン
19 流量調整バルブ
20 合流部
21 ラインミキサ
23 pH調整装置
24 pH測定装置
B ボイラ
E 電解処理水
M 海水
P プラント
W ボイラ排水
Claims (3)
- ボイラ排水を混合槽へ供給する排水ラインと、
前記排水ラインを流れる前記ボイラ排水のpHを測定するpH測定装置と、
前記排水ライン上に設けられ、前記ボイラ排水に前記ボイラ排水のpHを調整するpH調整剤を添加するpH調整装置と、
海水又は塩水を電気分解して次亜塩素酸を有する電解処理水を生成する電解装置と、
前記排水ラインと前記混合槽との合流部より上流に設けられ、前記電解装置で生成された次亜塩素酸を前記ボイラ排水に供給する供給ラインと、
前記pH測定装置の測定値に基づいて前記pH調整剤の添加量を制御する制御装置と、を有するアンモニア処理システム。 - 前記pH測定装置は、前記pH調整装置の下流側であって、前記pH調整装置によって添加された前記pH調整剤によって調整された前記ボイラ排水のpHが安定する位置に配置されている請求項1に記載のアンモニア処理システム。
- 前記排水ラインの上流側に設けられて前記ボイラ排水を貯留する貯留槽と、
前記貯留槽に貯留された前記ボイラ排水のpHを測定する貯留槽pH測定装置と、を有し、
前記制御装置は、前記貯留槽pH測定装置の測定値に基づいて前記電解装置にて生成される次亜塩素酸量を制御する請求項1又は請求項2に記載のアンモニア処理システム。
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KR1020177013814A KR101967079B1 (ko) | 2014-11-26 | 2015-11-20 | 암모니아 처리 시스템 |
SG11201704241YA SG11201704241YA (en) | 2014-11-26 | 2015-11-20 | Ammonia processing system |
CN201580063882.9A CN107001076A (zh) | 2014-11-26 | 2015-11-20 | 氨处理系统 |
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JP2014238637A JP6331145B2 (ja) | 2014-11-26 | 2014-11-26 | アンモニア処理システム |
JP2014-238637 | 2014-11-26 |
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JP (1) | JP6331145B2 (ja) |
KR (1) | KR101967079B1 (ja) |
CN (1) | CN107001076A (ja) |
SG (1) | SG11201704241YA (ja) |
TW (1) | TWI574921B (ja) |
WO (1) | WO2016084754A1 (ja) |
Cited By (1)
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WO2016167271A1 (ja) * | 2015-04-17 | 2016-10-20 | 三菱重工環境・化学エンジニアリング株式会社 | 次亜塩素酸供給装置及びボイラ排水の処理方法 |
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TWI648431B (zh) * | 2018-01-03 | 2019-01-21 | 莊政霖 | 電解裝置 |
JP7123650B2 (ja) * | 2018-06-18 | 2022-08-23 | 三菱重工業株式会社 | 復水設備、及びこれを備える蒸気タービンプラント |
CN110204017B (zh) * | 2019-05-16 | 2023-08-22 | 浙江浙能技术研究院有限公司 | 一种调节含氨废水pH值的电解处理系统及方法 |
JP6940713B1 (ja) * | 2021-05-18 | 2021-09-29 | 三菱重工環境・化学エンジニアリング株式会社 | 水素製造システム |
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- 2015-11-20 CN CN201580063882.9A patent/CN107001076A/zh active Pending
- 2015-11-20 KR KR1020177013814A patent/KR101967079B1/ko active IP Right Grant
- 2015-11-20 SG SG11201704241YA patent/SG11201704241YA/en unknown
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CN107001076A (zh) | 2017-08-01 |
KR20170073657A (ko) | 2017-06-28 |
SG11201704241YA (en) | 2017-06-29 |
KR101967079B1 (ko) | 2019-04-08 |
JP2016097387A (ja) | 2016-05-30 |
TWI574921B (zh) | 2017-03-21 |
JP6331145B2 (ja) | 2018-05-30 |
TW201632468A (zh) | 2016-09-16 |
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