WO2012144796A4 - 합성가스로부터 탄화수소를 제조하기 위한 반응장치 - Google Patents
합성가스로부터 탄화수소를 제조하기 위한 반응장치 Download PDFInfo
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- WO2012144796A4 WO2012144796A4 PCT/KR2012/002949 KR2012002949W WO2012144796A4 WO 2012144796 A4 WO2012144796 A4 WO 2012144796A4 KR 2012002949 W KR2012002949 W KR 2012002949W WO 2012144796 A4 WO2012144796 A4 WO 2012144796A4
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- heat exchange
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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- B01J16/00—Chemical processes in general for reacting liquids with non- particulate solids, e.g. sheet material; Apparatus specially adapted therefor
- B01J16/005—Chemical processes in general for reacting liquids with non- particulate solids, e.g. sheet material; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
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Definitions
- the present invention relates to a reactor system for producing hydrocarbons from syngas, and more particularly, to a reactor system for synthesizing hydrocarbons and oxygenates on a Fischer-Tropsch catalyst using syngas. To a reaction apparatus in which the catalyst can be easily replaced.
- CO, H 2 , - [CH 2 ] - n , and H 2 O are carbon monoxide, hydrogen, hydrocarbons having a chain length of n (carbon number n), and water.
- the selectivity of methane is increased and the selectivity of C 5+ (hydrocarbon having 5 or more carbon atoms) is relatively reduced, which is not suitable.
- Olefins, oxygenates (molecules containing oxygen atoms such as alcohols, aldehydes, ketones, etc.) as well as hydrocarbons in the form of paraffins having the above-described linear chains are also produced as by-products.
- One of the main objectives of the XTL process is to obtain liquid fuel, so it is important to optimize the ratio of cobalt-based catalyst, synthesis gas, temperature, pressure, etc. to produce linear hydrocarbons, especially C5 + Trend.
- iron-based catalysts are mainly used at an early stage. They are cheaper than cobalt, have low methane selectivity at high temperatures, have high olefin selectivity in hydrocarbons, and are used to produce olefinic products in addition to liquid fuels.
- Cobalt catalysts are mainly used to produce liquid fuels, produce less carbon dioxide, and have a longer lifetime. However, it is very expensive compared to iron, and the methane selectivity at high temperature is high, so it must be reacted at a relatively low temperature, and since it is expensive, a small amount should be dispersed on the surface of the support. Alumina, silica, titania and the like are used as supports, and the performance is improved by using precious metals such as Ru, Pt, and Re as a cocatalyst.
- the types of reactor considered to date include tubular fixed bed reactors, fluidized bed reactors, slurry phase reactors, micro-channel reactors equipped with heat exchangers, And multi-channel reactors.
- a circulating fluidized bed reactor and a fixed fluidized bed reactor are representative.
- the reaction characteristics and the distribution of the products vary depending on the reactor type, and accordingly, it should be appropriately selected according to the target end product.
- SASOL fluidized bed reactor
- Shell multitubular fixed bed reactor
- FPSO floating production, storage and offloading
- the catalytic reaction part and the heat exchange part are alternately stacked, and at least one part of the microchannel is composed of microchannels.
- the catalytic reacting part may be constituted by a slab type fixed bed while the heat exchanging part is constituted by a microchannel, or the reaction part may be constituted by a microchannel.
- a catalyst may be inserted into the channel and charged or may be attached to the inner wall of the reactor by a coating method or the like.
- These FT reactors are mainly suitable for producing diesel, lube oil, wax and the like, and the low-temperature F-T process is mainly operated.
- hydrocarbons having a boiling point higher than that of the diesel are produced in an amount of more than 60%. Therefore, a diesel is further produced through a subsequent process such as hydrocracking, and after a dewaxing process, Switch to use.
- the multitubular fixed-bed reactor and the slurry-phase reactor which are representative of the low-temperature F-T reaction, have various advantages, but they have a higher volume burden than the micro or multi-channel reactors.
- the multi-tubular fixed bed reactor is advantageous in that it does not have a burden of scale-up and has a small mechanical loss of the catalyst.
- the reactor since it is the reactor having the largest volume relative to the production volume, the volume occupied in the process is very large and the equipment cost and construction cost are large. And the heat and mass transfer efficiency is relatively low in the catalyst layer, which makes it difficult to control the reaction.
- the slurry-phase reactor is inexpensive in equipment cost and construction cost, and has good heat and mass transfer efficiency. However, it is difficult to design because it can be scaled up by interpreting the dynamics in a complex reactor, and there is mechanical loss of the catalyst due to friction or collision.
- a multi-channel reactor (hereinafter referred to as a microchannel reactor) is a reactor having a maximized heat transfer efficiency to allow reaction at a high space velocity.
- the reactor is relatively small in volume (1/5 to 1/2 of the conventional reaction process)
- the apparatus cost and the construction cost are reduced and the production amount can be increased by the concept of number-up, so that the scale-up is easy and the mechanical loss due to the friction or collision of the catalyst is insignificant.
- the present invention provides a reaction apparatus structured in a prefabricated manner in order to solve the problem of catalyst replacement, which is a disadvantage of a wall-coated multi-channel reactor in the reactor wall.
- the present invention provides a reaction apparatus for producing hydrocarbon from syngas, comprising: a heat exchanger for injecting a heat transfer medium, exchanging heat through a plurality of heat exchange plates, A dispersing device for distributing the injected heat transfer medium to each of the heat exchange plates; A cell in which one side is opened to insert heat exchange plates of the heat exchange unit into an internal reaction space, a reaction channel partitioned by the inserted heat exchange plates is formed, a reactant is injected into the reaction channel, and a reaction mixture is discharged; A fixing groove for fixing the inserted heat exchange plate on the opposite side of the reaction space into which the heat exchange plates are inserted; And a flange for fastening the heat exchange unit to the cell, and a catalyst material is attached to the heat exchange plate of the heat exchange unit before assembling the heat exchange unit and the cell.
- the heat exchanger is a plate-like type in which a heat transfer passage is formed, and a plurality of fins may be provided at regular intervals to increase the heat transfer area of each heat exchange plate, or a corrugated plate may be manufactured.
- the surface of the heat exchange plate is preferably subjected to an oxide film treatment so as to facilitate attachment of the catalyst material.
- An inert material may be filled in the upper and lower spaces of the reaction channel to distribute the injected reactant and the reaction mixture, or a dispersing plate may be installed to distribute the reaction mixture and the reaction mixture injected into the upper and lower portions of the reaction channel, An inert material is filled in the upper and lower spaces of the channel, and a dispersion plate can be installed at the upper and lower portions of the reaction channel.
- the catalytic material is adhered to the reaction channel at both ends of the reaction channel only on the side facing the heat exchange plate, and the width of the reaction channel may be less than 1/2 of the width of the reaction channel on which the catalytic material is attached.
- the reactors of the present invention can be connected in series or in parallel to form a module.
- an apparatus capable of inserting a heat exchange unit comprising a plurality of plate-shaped or corrugated plate-shaped heat exchange plates into a detachable form and inserting the heat exchange unit into a reaction unit,
- the heat transfer efficiency is maximized, and the heat exchanger is detached at the end of the catalyst life, so that the catalyst can be easily removed or reattached.
- FIG. 1 is an exploded perspective view illustrating a prefabricated multi-channel reactor according to a preferred embodiment of the present invention.
- FIG 3 is a partial detail view showing a fixing groove portion engaged with an end portion of the heat exchange plate.
- the reaction apparatus of the present invention for producing hydrocarbons from syngas comprises a heat exchange unit 10 in which a heat transfer medium is injected and heat-exchanged through a plurality of heat exchange plates 1 and then flows out; A dispersing device (5) for distributing the injected heat transfer medium to each of the heat exchange plates (1); And the reaction channels 8 (see FIG. 2) partitioned by the inserted heat exchange plates 1 are constituted by the heat exchange plates 1 of the heat exchange unit 10 inserted into the reaction space inside, A cell 20 into which a reactant is injected into the reaction channel 8 and into which a reaction mixture is discharged; A fixing groove 21 (see FIG.
- the heat exchange unit 1 of the heat exchange unit 10 is assembled before the heat exchange unit 10 and the cell 20 are assembled, The catalytic material is adhered thereto.
- the heat exchange plate 1 of the heat exchange unit 10 to which the catalyst is to be attached is inserted in the reaction space of the cell 20 in the direction of the arrow and then the flange 40 of the heat exchange unit 10 and the cell 20 are fastened to each other to constitute a reaction device.
- the heat exchange plate 1 of the heat exchange unit 10 is a heat exchange surface where substantial heat exchange takes place and a plurality of fins 2 are provided at equal intervals in the heat exchange plate 1 in order to increase the heat transfer area.
- a heat transfer path is formed in a suitable shape so that heat transfer medium can be uniformly transferred to the heat transfer medium.
- the heat transfer medium includes, for example, cooling water, steam, solid molten salt, silicon or fluorine-containing oil, and a mixture of biphenyl and biphenyl ether.
- the solid molten salt include a mixture of sodium nitrate and sodium nitrite in an appropriate ratio, but a variety of solid molten salts suitable for a desired temperature range can be selected and used.
- the above examples are a part of a typical heat transfer medium, and the present invention is not limited to the above examples.
- the heat exchanging part 10 is provided at one side of the flange 40 with an inlet 3 for a heat transfer medium into which the heat transfer medium is injected and an outlet 4 through which the heat transfer medium flows.
- the other end of the flange 40 is provided with a dispersing device 5 in which the heat transfer medium flowing from the injection port 3 is dispersed and a distributor is installed in the inner space of the dispersing device 5, And serves to evenly distribute the heat transfer fluid to the heat exchange surfaces inside the heat exchange plate (1).
- the distribution device 5 also serves to prevent the reaction gas from leaking when fastened to the cell 20, and a gasket may be installed around the front or rear of the distribution device 5 if necessary.
- the heat exchanging part 10 is filled with a heat transfer fluid from the first heat transfer plate 1 and is discharged through the outlet 4 after heat exchange in the first heat transfer plate 1.
- the catalyst material for the reaction is attached to each surface of the heat exchange plate 1 by a method such as a wash coat.
- the cell 20 includes an upper space 7 and a lower space 9 in the form of a tetrahedron cone formed in an opposite direction to the reaction channels 8 and upper and lower portions of the reaction channel 8, (7) is provided with an inlet (6) for injecting a reactant into a vertex of the cone, and an outlet (11) through which the reaction mixture exits from the vertex of the cone is formed in the lower space (9).
- the upper space 7 and the lower space 9 can be filled with a particle layer of inert material for dispersion of the reaction mixture.
- inert material for example, alumina, Raschig ring, glass bead and the like can be filled.
- the dispersing plates 12 and 13 may be additionally provided, and if necessary, both of the inert material and the dispersion plates 12, 13 may be used.
- the dispersion plates 12 and 13 may be made of, for example, a metal foam, a plate-like filter (metal or ceramic), or the like.
- the reaction channel 8 is a reaction space partitioned by the heat transfer plates 1, and catalyst materials are attached to both sides of the reaction channel 8 on both sides except for both ends thereof.
- the reaction channels 8 at both ends are attached to the catalytic material only on the side facing the heat exchange plate 1.
- the widths of the reaction channels 8 at both the left and right ends are designed to be equal to or less than half the width of the other reaction channels in the middle.
- the reaction between the heat exchange plates 1 and the reaction channel 8 is not completely blocked, and channeling of the unreacted mixture may occur between the open spaces.
- the opposite side of the reaction space of the cell 20 into which the heat exchange plates 1 are inserted that is, the opposite side of the reaction channel 8 on the side to insert the heat exchange plate 1
- the fixing groove 21 into which the tip of the heat exchange plate 1 is inserted and fixed can be elongated to prevent channeling.
- the heat exchange plate 1 is not limited to a plate type in which a plurality of fins 2 are provided as shown in Fig. Any shape that can increase the heat transfer area, such as a corrugated plate, may be used.
- FIG. 1 one cell unit of the entire reaction system is shown, and the reaction unit of the present invention may be configured as one module by connecting the cells in series or in parallel.
- the module thus configured is relatively easy to scale-up with the concept of number-up.
- the reactivity is very high compared to the reactor volume, so that a high-performance, compact reactor configuration is possible. Therefore, it is suitable for a small to medium-sized gas field having a limited amount of gas, and can sufficiently exhibit its functions even in specialized applications such as FPSO.
- a catalyst material is adhered to a heat transfer surface and reacted rather than filling the catalyst particles to maximize heat transfer efficiency.
- the path has a large heat transfer resistance in the order of catalytic phase (reaction heat generation) ⁇ gas phase ⁇ heat transfer surface ⁇ heat transfer medium, in particular, thermal efficiency is low due to low thermal conductivity in the vapor phase.
- the heat transfer path is simplified to a catalyst phase (reaction heat generation) ⁇ heat transfer surface ⁇ heat transfer medium, .
Abstract
Description
Claims (9)
- 합성가스로부터 탄화수소를 제조하기 위한 반응장치로서,열전달 매체가 주입되어 촉매 물질이 부착된 다수의 열교환판을 거쳐 열교환된 후 유출되는 열교환부;상기 주입된 열전달 매체를 상기 열교환판의 각각으로 배분하는 분산장치;일측이 개방되어 내부의 반응 공간으로 상기 열교환부의 열교환판들이 삽입되며, 상기 삽입된 열교환판들에 의해 구획된 반응채널이 구성되며, 상기 반응채널로 반응물이 주입되고, 반응 혼합물이 배출되는 셀;상기 열교환판들이 삽입되는 상기 반응공간의 맞은 편에 상기 삽입된 열교환판을 고정하는 고정홈; 및상기 열교환부와 상기 셀을 체결하는 플랜지를 포함하는 반응장치.
- 제 1 항에 있어서,상기 열교환기는 내부에 열전달 유로를 형성하는 판상형으로, 등간격으로 핀이 설치되거나, 또는 주름 판상형(corrugated plate) 형태로 제작되는 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 열교환판의 표면은 촉매물질의 부착이 용이하도록 산화막 처리한 것을 특징으로 하는 반응장치.
- 제 2 항에 있어서,상기 열교환판의 표면은 촉매물질의 부착이 용이하도록 산화막 처리한 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 반응채널의 상부와 하부의 공간에는 상기 주입된 반응물과 반응 혼합물의 분배를 위해 불활성 물질이 채워지는 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 반응채널의 상부와 하부에 상기 주입된 반응물과 반응 혼합물의 분배를 위해 분산판이 설치되는 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 반응채널의 상부와 하부의 공간에는 상기 주입된 반응물과 반응 혼합물의 분배를 위해 불활성 물질이 채워지고,상기 반응채널의 상부와 하부에 상기 주입된 반응물과 반응 혼합물의 분배를 위해 분산판이 설치되는 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 반응채널 중 양쪽 끝의 반응채널은 상기 열교환판과 면하는 쪽에만 상기 촉매물질이 부착되며, 이때의 폭은 다른 반응채널의 폭보다 1/2 이하 인 것을 특징으로 하는 반응장치.
- 제 1 항에 있어서,상기 반응장치를 직렬 또는 병렬로 연결하여 모듈로 구성한 것을 특징으로 하는 반응장치.
Priority Applications (5)
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CN201280019330.4A CN103476907B (zh) | 2011-04-19 | 2012-04-18 | 由合成气制备烃的反应器系统 |
CA2832364A CA2832364C (en) | 2011-04-19 | 2012-04-18 | Reactor system for producing hydrocarbons from synthetic gas |
EP12774203.9A EP2700701A4 (en) | 2011-04-19 | 2012-04-18 | REACTION DEVICE FOR THE PRODUCTION OF HYDROCARBONS FROM A SYNTHESEGAS |
AU2012246877A AU2012246877B2 (en) | 2011-04-19 | 2012-04-18 | Reactor system for producing hydrocarbons from synthetic gas |
US14/111,384 US9446370B2 (en) | 2011-04-19 | 2012-04-18 | Reactor system for producing hydrocarbons from synthetic gas |
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KR10-2011-0036171 | 2011-04-19 | ||
KR1020110036171A KR101297597B1 (ko) | 2011-04-19 | 2011-04-19 | 합성가스로부터 탄화수소를 제조하기 위한 반응장치 |
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WO2012144796A2 WO2012144796A2 (ko) | 2012-10-26 |
WO2012144796A3 WO2012144796A3 (ko) | 2013-01-03 |
WO2012144796A4 true WO2012144796A4 (ko) | 2013-02-28 |
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US (1) | US9446370B2 (ko) |
EP (1) | EP2700701A4 (ko) |
KR (1) | KR101297597B1 (ko) |
CN (1) | CN103476907B (ko) |
AU (1) | AU2012246877B2 (ko) |
CA (1) | CA2832364C (ko) |
WO (1) | WO2012144796A2 (ko) |
Cited By (1)
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CN110860268A (zh) * | 2018-08-28 | 2020-03-06 | 美国分子工程股份有限公司 | 结构材料水热生长反应器 |
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CN104096525B (zh) * | 2014-08-07 | 2015-10-28 | 淄博市临淄环宇经贸有限公司 | 一种实现规模化生产的微通道反应器 |
DE102017001567B4 (de) * | 2017-02-20 | 2022-06-09 | Diehl Aerospace Gmbh | Verdampfer und Brennstoffzellenanordnung |
CN108176335B (zh) * | 2018-03-07 | 2024-01-05 | 厦门大学 | 具有孔槽复合微通道多孔金属反应载体的串联式微反应器 |
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DE3107010C2 (de) * | 1981-02-25 | 1985-02-28 | Dieter Christian Steinegg-Appenzell Steeb | Metallkühler zum Kühlen eines unter hohem Druck durchströmenden Fluids durch Luft |
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JPH10281015A (ja) * | 1997-04-02 | 1998-10-20 | Calsonic Corp | Egrガス冷却装置 |
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DE60007811T2 (de) * | 1999-08-23 | 2004-11-25 | Nippon Shokubai Co., Ltd. | Verfahren zur Verhinderung von Verstopfungen in einem Plattenwärmetauscher |
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DE10302948A1 (de) * | 2003-01-24 | 2004-08-05 | Behr Gmbh & Co. Kg | Wärmeübertrager, insbesondere Abgaskühler für Kraftfahrzeuge |
US20040168791A1 (en) * | 2003-02-27 | 2004-09-02 | Alstom (Switzerland) Ltd. | Integrated core/casing plate heat exchanger |
DE10317451A1 (de) | 2003-04-16 | 2004-11-18 | Degussa Ag | Reaktor für heterogen katalysierte Reaktionen |
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CN100510606C (zh) * | 2004-09-28 | 2009-07-08 | 株式会社T.Rad | 换热器 |
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GB0725140D0 (en) | 2007-12-24 | 2008-01-30 | Compactgtl Plc | Catalytic Reactor |
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2011
- 2011-04-19 KR KR1020110036171A patent/KR101297597B1/ko active IP Right Grant
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2012
- 2012-04-18 AU AU2012246877A patent/AU2012246877B2/en not_active Ceased
- 2012-04-18 US US14/111,384 patent/US9446370B2/en active Active
- 2012-04-18 CA CA2832364A patent/CA2832364C/en not_active Expired - Fee Related
- 2012-04-18 CN CN201280019330.4A patent/CN103476907B/zh not_active Expired - Fee Related
- 2012-04-18 EP EP12774203.9A patent/EP2700701A4/en not_active Withdrawn
- 2012-04-18 WO PCT/KR2012/002949 patent/WO2012144796A2/ko active Application Filing
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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CN110860268A (zh) * | 2018-08-28 | 2020-03-06 | 美国分子工程股份有限公司 | 结构材料水热生长反应器 |
CN110860268B (zh) * | 2018-08-28 | 2021-10-08 | 美国分子工程股份有限公司 | 结构材料水热生长反应器 |
Also Published As
Publication number | Publication date |
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CN103476907A (zh) | 2013-12-25 |
AU2012246877B2 (en) | 2015-09-17 |
EP2700701A2 (en) | 2014-02-26 |
KR20120118664A (ko) | 2012-10-29 |
CA2832364A1 (en) | 2012-10-26 |
US9446370B2 (en) | 2016-09-20 |
CA2832364C (en) | 2016-09-13 |
KR101297597B1 (ko) | 2013-08-19 |
AU2012246877A1 (en) | 2013-10-24 |
EP2700701A4 (en) | 2014-12-10 |
WO2012144796A2 (ko) | 2012-10-26 |
WO2012144796A3 (ko) | 2013-01-03 |
CN103476907B (zh) | 2015-05-27 |
US20140044614A1 (en) | 2014-02-13 |
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