WO2013185400A1 - 一种用乙炔和二氯乙烷制备氯乙烯的方法 - Google Patents
一种用乙炔和二氯乙烷制备氯乙烯的方法 Download PDFInfo
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- WO2013185400A1 WO2013185400A1 PCT/CN2012/078540 CN2012078540W WO2013185400A1 WO 2013185400 A1 WO2013185400 A1 WO 2013185400A1 CN 2012078540 W CN2012078540 W CN 2012078540W WO 2013185400 A1 WO2013185400 A1 WO 2013185400A1
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- vinyl chloride
- dichloroethane
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- gas
- cold
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/35—Preparation of halogenated hydrocarbons by reactions not affecting the number of carbon or of halogen atoms in the reaction
- C07C17/354—Preparation of halogenated hydrocarbons by reactions not affecting the number of carbon or of halogen atoms in the reaction by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/07—Preparation of halogenated hydrocarbons by addition of hydrogen halides
- C07C17/08—Preparation of halogenated hydrocarbons by addition of hydrogen halides to unsaturated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/07—Preparation of halogenated hydrocarbons by addition of hydrogen halides
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
Definitions
- the present invention relates to a process for producing vinyl chloride, and more particularly to a process for producing vinyl chloride from ethyl bromide and dichloroethane.
- Polyvinyl chloride is one of the five general-purpose plastics, and its output is second only to polyethylene (PE), ranking second in the world in plastics production, with an annual output of more than 40 million tons.
- the earliest synthetic method of polyvinyl chloride is the block method, that is, under the catalysis of mercuric chloride, ethylene and hydrogen chloride are added to synthesize vinyl chloride, and vinyl chloride is polymerized to obtain polyvinyl chloride.
- This method has serious mercury contamination problems due to the use of mercury chloride as a catalyst.
- the ethylene process was changed to vinyl chloride, and in the 1980s, the process of ethylene glycol was basically eliminated. Due to the tight ethylene resources in China and the abundant resources of calcium carbide, PVC production is still dominated by the B block method. However, with the continuous expansion of the production capacity of the block method, it faces enormous environmental pollution pressure. Domestic counterparts have been working on mercury-free catalysts in recent years and have made certain achievements.
- the addition reaction of ethylbenzene and hydrogen chloride is an exothermic reaction, while the dehydrochlorination of dichloroethane is an endothermic reaction, and two reactions are coupled together.
- the micro-exothermic reaction is formed, and the thermal effect of the reaction is not large. Therefore, the reactor can adopt an adiabatic reactor, and the reaction temperature is controlled within an appropriate range by means of intermediate cold stimulation, so that the reactor structure is greatly simplified.
- a part of hydrogen chloride is produced as a by-product.
- the method for preparing vinyl chloride from ethyl dichloroethane of the present invention comprises the following steps:
- step 4) After cooling the mixture produced in the reaction of step 3) to 30 to 50 ° C, pressurize to 0.4 to 1.0 MPa, then cool to room temperature, and then further freeze to _25 to 15 ° C for liquefaction separation, not liquefied. Gas recycling and recycling;
- the liquid obtained by liquefying in the step 4) is sent to a rectification column for rectification to obtain a vinyl chloride monomer which meets the polymerization requirements, that is, the vinyl chloride of the present invention is obtained.
- the molar ratio of the block, the dichloroethane and the hydrogen chloride is 1: (0.3 ⁇ 0.6): (0 ⁇ 05 ⁇ 0 ⁇ 20).
- the preheating temperature is 150 to 230 °C.
- the catalyst adopts an activated carbon supported ruthenium salt catalyst; preferably, the activated carbon supported ruthenium salt catalyst generally uses activated carbon supported ruthenium chloride; the activated carbon supported ruthenium chloride catalyst of the invention
- the preparation method can be referred to the Chinese patent application No. 201110330158.1: a catalyst for preparing vinyl chloride, a preparation method thereof and use thereof.
- the reactor adopts a multi-stage cold-excited fixed-bed reactor; preferably, the multi-stage cold-excited fixed-bed reactor adopts a reaction bed of 2 to 5 stages, and the intermediate is alternated. 1 ⁇ 4 times of cold shock is used, and 1 cold shock is used between the two stages of reaction; optimally, the multistage cold-excited fixed bed reactor adopts a reaction bed of 3 ⁇ 4 stages for reaction, and alternately adopts 2 ⁇ Three times of cold shock, and one cold shock was used between the two reactions.
- the cold shock uses a cold raw material gas as a cold shock medium, or is directly sprayed into liquid dichloroethane for cold shock; It is best to use direct injection of liquid dichloroethane for cold shock to reduce the temperature of the reaction gas to meet the inlet temperature requirements.
- the above-mentioned cold shock medium uses a cold raw material gas which is a mixture of one or more of cold block, dichloroethane and hydrogen chloride.
- the reaction bed inlet temperature of the multi-stage cold-excited fixed-bed reactor is 150 to 230 ° C
- the reaction bed outlet temperature of the multi-stage cold-excited fixed-bed reactor is 220 to 280 ° C
- the conversion rate of raw materials can reach 70% or more, even up to 80%.
- the inlet temperature of the reaction bed of the above various stages may be any value of 150 ⁇ 230 ° C
- the outlet temperature of the reaction bed of each stage may also be any value of 220 to 280 ° C
- the inlet temperature of the reaction bed of each stage may be different.
- the outlet temperature can also be different and can be adjusted according to actual needs.
- the feed rate of the raw material mixture gas is controlled to be 10 to 100 cubic meters of raw material mixture per cubic meter of catalyst per hour;
- the pressure of the reaction may be 0 to 0.12 MPa (gauge pressure), the pressure The number displayed for the gauge pressure, and 0 MPa means no pressure, it is normal pressure.
- the reaction pressure in the reactors of the above stages may be any one of 0 to 0.12 MPa, and the reaction pressures in the reactors of the respective stages may be different, and may be adjusted according to actual needs.
- the present invention Compared with the existing one-block process, the present invention has the following outstanding advantages:
- VCM vinyl chloride
- FIG. 1 is a schematic view showing the structure of a multi-stage cold-excited fixed bed reactor of a secondary cold shock three-stage reaction according to an embodiment of the present invention.
- each mark is: 1 primary reactor;
- FIG. 2 is a schematic view showing the structure of a multi-stage cold-excited fixed-bed reactor in which multi-stage reactions are integrated according to an embodiment of the present invention.
- each mark is: 13 raw material gas inlet;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor uses a multi-stage cold-excited fixed-bed reactor with a two-stage reaction with a single cold shock.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 150 ° C, and the outlet temperature was 280 ° C, so that the conversion rate of raw materials (in terms of E) reached 80%.
- the feed gas velocity of the raw material mixture is controlled to treat 100 cubic meters of the raw material mixture per cubic catalyst per hour, and the reaction pressure is controlled at 0.12 MPa (gauge pressure).
- step 4) Cool the mixture produced in step 3) to 50 ° C, pressurize to 1.0 MPa, cool to room temperature, and then further freeze to 15 ° C for liquefaction separation, unliquefied gas recovery and recycling;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor uses a multi-stage cold-excited fixed-bed reactor with a 5-stage reaction and 4 cold-excitations in the middle.
- the cold shock medium uses a cold raw material gas to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 230 ° C, and the outlet temperature was 270 ° C, so that the conversion rate of raw materials (in terms of E) reached 85%.
- the feed gas mixture is controlled to have an intake gas velocity of 50 cubic meters of raw material per cubic meter per hour, and the reaction pressure is controlled at O.10 MPa (gauge pressure).
- step 4) Cool the mixture produced in the reaction of step 3) to 30 ° C, pressurize to 0.4 MPa, cool to room temperature, and then further freeze to -25. C is liquefied and separated, and the unliquefied gas is recycled and recycled;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor uses a multi-stage cold-excited fixed-bed reactor with a 3-stage reaction and 2 times of cold stimulation (see the second shown in Figure 1).
- the multi-stage cold-excited fixed-bed reactor of the cold-shock three-stage reaction can also integrate the multi-stage reaction together, as shown in Fig. 2, the multi-stage cold-excited fixed-bed reactor in which the multi-stage reaction is integrated.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 160 ° C, and the outlet temperature was 250 ° C, so that the conversion rate of raw materials (in terms of E) reached 70%.
- the feed gas velocity of the raw material mixture is controlled to treat 70 cubic meters of the raw material mixture per cubic catalyst per hour, and the reaction pressure is controlled at 0.08 MPa (gauge pressure).
- step 4) Cool the mixture produced in step 3) to 40 ° C, pressurize to 0.6 MPa, cool to room temperature, and then further freeze to 0 ° C for liquefaction separation, unliquefied gas recovery and recycling;
- step 5 The liquid obtained by liquefying in step 4) is sent to the rectification column for rectification, and a vinyl chloride monomer meeting the polymerization requirements can be obtained.
- the above-mentioned secondary cold shock three-stage reaction multi-stage cold-excited fixed-bed reactor (shown in FIG. 1) comprises a first-stage reactor 1, a first-stage chiller 2, a second-stage reactor 3, two a stage chiller 4 and a third stage reactor 5, the top of the first stage reactor 1 is provided with a feed gas inlet 7, and the top of the first stage chiller 2 is provided with a cold shock medium inlet 8, a secondary chiller 4
- the top of the first stage is provided with a cold shock medium inlet 9, the bottom of the first stage reactor 1 and the bottom of the first stage chiller 2 are connected by a pipe, and the top of the primary chiller 2 is also connected to the top of the secondary reactor 3 via a pipe.
- the bottom of the secondary reactor 3 and the bottom of the secondary chiller 4 are connected by a pipe, and the top of the secondary chiller 4 is also connected to the top of the tertiary reactor 5 via a pipe, and the bottom of the tertiary reactor 5 is provided.
- the multi-stage cold-excited fixed-bed reactor (shown in FIG. 2) in which the above-mentioned multi-stage reaction is integrated, the multi-stage cold-excited fixed-bed reactor is provided with a raw material gas inlet 13 at the top and a product gas outlet 17 at the bottom.
- the multistage cold shock fixed bed reactor in which the plurality of stages of reaction are integrated includes a first reaction stage 18 (or a first stage reactor 18) in order from top to bottom, and a first communication stage 18 a chiller 19, a second reaction section 20 (also referred to as a second stage reactor 20) in communication with the first chiller 19, a second chiller 21 in communication with the second reaction section 20, and a second a third reaction section 22 (also referred to as a third stage reactor 22) in which the chiller 21 is in communication, and the first reaction section 18, the second reaction section 20, and the third reaction section 22 are filled with a catalyst 14, first One side of the chiller 19 is provided with a cold shock medium inlet 15, and one side of the second chiller 21 is provided with a cold shock medium inlet 16.
- the reactor uses a multi-stage cold-excited fixed bed reactor, generally using a three-stage reaction with two cold shocks in the middle.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 170 °C and the outlet temperature was 240 °C, so that the conversion rate of raw materials (in terms of E) reached 75%.
- the feed gas velocity of the raw material mixture is controlled to treat 40 cubic meters of the raw material mixture per cubic catalyst per hour, and the reaction pressure is controlled at 0.05 MPa (gauge pressure).
- step 4) The mixture gas produced in the reaction of step 3) is cooled to 35 ° C, pressurized to 0.7 MPa, cooled to normal temperature, and then further chilled to 5 ° C for liquefaction separation, and the liquefied gas is recycled and recycled;
- Example 5 The liquid obtained by liquefying in step 4) is sent to the rectification column for rectification, and a vinyl chloride monomer meeting the polymerization requirements can be obtained.
- Example 5 The liquid obtained by liquefying in step 4) is sent to the rectification column for rectification, and a vinyl chloride monomer meeting the polymerization requirements can be obtained.
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor was a multi-stage cold-excited fixed-bed reactor with a 4-stage reaction and three cold-radical reactions.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 180 ° C, and the outlet temperature was 230 ° C, so that the conversion rate of raw materials (in terms of E) reached 70%.
- the feed rate of the raw material mixture is controlled to treat 40 cubic meters of the raw material mixture per cubic meter per hour, and the reaction pressure is controlled at 0.02 MPa (gauge pressure).
- step 4) Cooling the mixture produced in the reaction of step 3) to 50 ° C, pressurizing to 0.6 MPa, cooling to normal temperature, and then further freezing to 10 ° C for liquefaction separation, recycling of unliquefied gas;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor was a multi-stage cold-excited fixed-bed reactor with a 3-stage reaction and 2 cold-radicals in the middle.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 165 ° C, and the outlet temperature was 220 ° C, so that the conversion rate of raw materials (in terms of E) reached 75%.
- the feed gas velocity of the raw material mixture is controlled to treat 10 cubic meters of the raw material mixture per cubic catalyst per hour, and the reaction pressure is normal pressure.
- step 4) The mixture gas produced in the reaction of step 3) is cooled to 30 ° C, pressurized to 0.6 MPa, cooled to normal temperature, and further chilled to -5 ° C for liquefaction separation, and the liquefied gas is recycled and recycled;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor uses a multi-stage cold-excited fixed-bed reactor with a 5-stage reaction and 4 cold-excitations in the middle.
- the cold shock is carried out by spraying liquid dichloroethane to lower the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 230 ° C, and the outlet temperature was 270 ° C, so that the conversion rate of raw materials (in terms of E) reached 85%.
- the feed rate of the raw material mixture is controlled to 50 cubic meters of raw material mixture per hour of the catalyst, and the reaction pressure is controlled at O.10 MPa (gauge pressure).
- step 4) Cool the mixture produced in the reaction of step 3) to 30 ° C, pressurize to 0.4 MPa, cool to room temperature, and then further freeze to -25. C is liquefied and separated, and the unliquefied gas is recycled and recycled;
- the preheated raw material mixture is passed to a reactor equipped with a catalyst, and the catalyst used is activated carbon supported ruthenium chloride.
- the reactor was a multi-stage cold-excited fixed-bed reactor with a 4-stage reaction and 3 cold-radicals in the middle. Cold shock medium using cold original
- the feed gas reduces the temperature of the reaction gas to meet the inlet temperature requirements.
- the reaction bed inlet temperature was controlled at 180 ° C, and the outlet temperature was 230 ° C, so that the conversion rate of raw materials (in terms of E) reached 80%.
- the feed gas velocity of the raw material mixture is controlled to treat 40 cubic meters of the raw material mixture per cubic catalyst per hour, and the reaction pressure is controlled at 0.02 MPa (gauge pressure).
- step 4) Cooling the mixture produced in the reaction of step 3) to 50 ° C, pressurizing to 0.6 MPa, cooling to normal temperature, and then further freezing to 10 ° C for liquefaction separation, recycling of unliquefied gas;
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IN10674DEN2014 IN2014DN10674A (zh) | 2012-06-11 | 2012-07-12 | |
US14/406,931 US9371259B2 (en) | 2012-06-11 | 2012-07-12 | Method for preparing vinyl chloride from acetylene and dichlorethane |
JP2015515365A JP5974169B2 (ja) | 2012-06-11 | 2012-07-12 | アセチレン及びジクロロエタンを用いて塩化ビニルを生成する方法 |
ZA2014/09015A ZA201409015B (en) | 2012-06-11 | 2014-12-09 | Method for preparing vinyl chloride with acetylene and dichlorethane |
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CN201210191433.0 | 2012-06-11 | ||
CN201210191433.0A CN102675035B (zh) | 2012-06-11 | 2012-06-11 | 一种用乙炔和二氯乙烷制备氯乙烯的方法 |
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US (1) | US9371259B2 (zh) |
JP (1) | JP5974169B2 (zh) |
CN (1) | CN102675035B (zh) |
IN (1) | IN2014DN10674A (zh) |
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
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US20130204052A1 (en) * | 2011-10-26 | 2013-08-08 | Zhongke Yigong (Xiamen) Chemical Technology Co. Ltd. | Catalyst for preparing vinyl chloride, methods of preparation and application thereof |
US9371259B2 (en) | 2012-06-11 | 2016-06-21 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Method for preparing vinyl chloride from acetylene and dichlorethane |
CN112844460A (zh) * | 2019-11-27 | 2021-05-28 | 中国科学院大连化学物理研究所 | 乙炔与二氯乙烷耦合反应制备氯乙烯的催化剂及其应用 |
CN113426490A (zh) * | 2021-06-24 | 2021-09-24 | 宁夏新龙蓝天科技股份有限公司 | 一种添加二氯乙烷制作无汞触媒的方法 |
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CN102911007B (zh) * | 2012-11-09 | 2015-04-01 | 中科易工(上海)化学科技有限公司 | 一种氯乙烯的无汞合成方法 |
CN103408392A (zh) * | 2013-07-17 | 2013-11-27 | 北京化工大学 | 聚氯乙烯环形路线生产方法 |
CN104326865B (zh) * | 2014-10-11 | 2016-03-23 | 中国科学院上海高等研究院 | 一种催化乙炔二氯乙烷制备氯乙烯的方法 |
CN104326867B (zh) * | 2014-10-16 | 2016-03-16 | 中科易工(上海)化学科技有限公司 | 一种乙炔和二氯乙烷无汞催化合成氯乙烯工艺尾气中氯乙烯的分离回收方法 |
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CN106391078B (zh) * | 2015-07-31 | 2019-06-28 | 天津大学 | 一种用于二氯乙烷和乙炔一步法制备氯乙烯的催化剂及制备方法及用途 |
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CN107129423A (zh) * | 2017-04-26 | 2017-09-05 | 安徽华塑股份有限公司 | 一种纯化氯乙烯气体的方法 |
CN109293469B (zh) * | 2018-10-10 | 2021-06-08 | 青岛科技大学 | 一种甲苯二异氰酸酯副产氯化氢气体与乙炔气体混合冷冻脱水的方法 |
CN110052222A (zh) * | 2019-05-20 | 2019-07-26 | 陕西金泰氯碱化工有限公司 | 一种冷激式无汞催化氯乙烯合成的工艺方法 |
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- 2012-07-12 WO PCT/CN2012/078540 patent/WO2013185400A1/zh active Application Filing
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2014
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US9056305B2 (en) * | 2011-10-26 | 2015-06-16 | Shanghai Cas Advanced Research Institute | Catalyst for preparing vinyl chloride, methods of preparation and application thereof |
US9371259B2 (en) | 2012-06-11 | 2016-06-21 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Method for preparing vinyl chloride from acetylene and dichlorethane |
CN112844460A (zh) * | 2019-11-27 | 2021-05-28 | 中国科学院大连化学物理研究所 | 乙炔与二氯乙烷耦合反应制备氯乙烯的催化剂及其应用 |
CN112844460B (zh) * | 2019-11-27 | 2022-06-03 | 中国科学院大连化学物理研究所 | 乙炔与二氯乙烷耦合反应制备氯乙烯的催化剂及其应用 |
CN113426490A (zh) * | 2021-06-24 | 2021-09-24 | 宁夏新龙蓝天科技股份有限公司 | 一种添加二氯乙烷制作无汞触媒的方法 |
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JP5974169B2 (ja) | 2016-08-23 |
US9371259B2 (en) | 2016-06-21 |
CN102675035A (zh) | 2012-09-19 |
ZA201409015B (en) | 2017-06-28 |
IN2014DN10674A (zh) | 2015-08-28 |
JP2015522555A (ja) | 2015-08-06 |
CN102675035B (zh) | 2014-04-09 |
US20150141713A1 (en) | 2015-05-21 |
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