WO2010013958A2 - 천연가스와 이산화탄소로부터 합성가스 제조를 위한 촉매 및 이의 제조방법 - Google Patents
천연가스와 이산화탄소로부터 합성가스 제조를 위한 촉매 및 이의 제조방법 Download PDFInfo
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- WO2010013958A2 WO2010013958A2 PCT/KR2009/004256 KR2009004256W WO2010013958A2 WO 2010013958 A2 WO2010013958 A2 WO 2010013958A2 KR 2009004256 W KR2009004256 W KR 2009004256W WO 2010013958 A2 WO2010013958 A2 WO 2010013958A2
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- Prior art keywords
- catalyst
- reaction
- mgalo
- reforming reaction
- synthesis
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- 239000003054 catalyst Substances 0.000 title claims abstract description 176
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 94
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 65
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 57
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 40
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 39
- 239000007789 gas Substances 0.000 title claims abstract description 34
- 239000003345 natural gas Substances 0.000 title claims abstract description 13
- 238000002360 preparation method Methods 0.000 title abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 136
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 114
- 238000006057 reforming reaction Methods 0.000 claims abstract description 64
- 238000000034 method Methods 0.000 claims abstract description 51
- 229910004625 Ce—Zr Inorganic materials 0.000 claims abstract description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000000629 steam reforming Methods 0.000 claims abstract description 11
- 238000002407 reforming Methods 0.000 claims description 28
- 230000008859 change Effects 0.000 claims description 21
- 239000002243 precursor Substances 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 17
- 229910052684 Cerium Inorganic materials 0.000 claims description 16
- 229910052751 metal Inorganic materials 0.000 claims description 16
- 239000002184 metal Substances 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 12
- 239000004480 active ingredient Substances 0.000 claims description 11
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 10
- 230000009467 reduction Effects 0.000 claims description 10
- 229910052726 zirconium Inorganic materials 0.000 claims description 8
- 238000001354 calcination Methods 0.000 claims description 6
- 159000000021 acetate salts Chemical class 0.000 claims description 5
- 150000004679 hydroxides Chemical class 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 4
- 229910002651 NO3 Inorganic materials 0.000 claims description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 4
- 229910052749 magnesium Inorganic materials 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 3
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 2
- 239000001099 ammonium carbonate Substances 0.000 claims description 2
- 235000012501 ammonium carbonate Nutrition 0.000 claims description 2
- 150000002823 nitrates Chemical class 0.000 claims description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 2
- 239000011734 sodium Substances 0.000 claims description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 abstract description 101
- 229910052759 nickel Inorganic materials 0.000 abstract description 28
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 17
- 239000001257 hydrogen Substances 0.000 abstract description 15
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 10
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 230000002779 inactivation Effects 0.000 abstract description 3
- 230000009257 reactivity Effects 0.000 abstract description 3
- 239000007799 cork Substances 0.000 abstract 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 39
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 34
- 230000000694 effects Effects 0.000 description 25
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- 239000010949 copper Substances 0.000 description 15
- 239000011148 porous material Substances 0.000 description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 14
- 229910052799 carbon Inorganic materials 0.000 description 14
- 230000009849 deactivation Effects 0.000 description 14
- 230000002829 reductive effect Effects 0.000 description 14
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 13
- 230000008021 deposition Effects 0.000 description 12
- 230000000052 comparative effect Effects 0.000 description 11
- 230000007423 decrease Effects 0.000 description 11
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical group [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 description 11
- ZZBAGJPKGRJIJH-UHFFFAOYSA-N 7h-purine-2-carbaldehyde Chemical compound O=CC1=NC=C2NC=NC2=N1 ZZBAGJPKGRJIJH-UHFFFAOYSA-N 0.000 description 7
- 230000035484 reaction time Effects 0.000 description 7
- 239000002904 solvent Substances 0.000 description 7
- 230000032683 aging Effects 0.000 description 6
- 238000000975 co-precipitation Methods 0.000 description 6
- 238000010304 firing Methods 0.000 description 6
- 238000005470 impregnation Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- OERNJTNJEZOPIA-UHFFFAOYSA-N zirconium nitrate Chemical compound [Zr+4].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O OERNJTNJEZOPIA-UHFFFAOYSA-N 0.000 description 6
- 229910052802 copper Inorganic materials 0.000 description 5
- 238000001035 drying Methods 0.000 description 5
- 238000011160 research Methods 0.000 description 5
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- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 4
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical group [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 4
- VGBWDOLBWVJTRZ-UHFFFAOYSA-K cerium(3+);triacetate Chemical compound [Ce+3].CC([O-])=O.CC([O-])=O.CC([O-])=O VGBWDOLBWVJTRZ-UHFFFAOYSA-K 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- 238000002441 X-ray diffraction Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052700 potassium Inorganic materials 0.000 description 3
- 239000011591 potassium Substances 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 238000002453 autothermal reforming Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
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- 229910052593 corundum Inorganic materials 0.000 description 2
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- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 101001131990 Homo sapiens Peroxidasin homolog Proteins 0.000 description 1
- 102100034601 Peroxidasin homolog Human genes 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
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- 229910021529 ammonia Inorganic materials 0.000 description 1
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- 239000003225 biodiesel Substances 0.000 description 1
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- DALUDRGQOYMVLD-UHFFFAOYSA-N iron manganese Chemical compound [Mn].[Fe] DALUDRGQOYMVLD-UHFFFAOYSA-N 0.000 description 1
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- -1 nickel aluminate Chemical class 0.000 description 1
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Definitions
- the present invention relates to a catalyst for producing a synthesis gas from natural gas and carbon dioxide, a method for preparing the same, and a method for preparing a synthesis gas that can be used for methanol synthesis or Fischer-Tropsch reaction using the catalyst.
- the methods for producing syngas using natural gas include steam reforming of methane (SRM), partial oxidation of methane (POM) using oxygen, and carbon dioxide reforming of methane.
- SRM steam reforming of methane
- POM partial oxidation of methane
- CO carbon dioxide reforming of methane.
- the carbon monoxide and hydrogen (H 2 / CO) ratios generated from each reforming reaction can be used differently depending on the optimally required ratios in subsequent processes.
- the H 2 / CO ratio can be obtained at 3 or more, and is a reforming reaction suitable for hydrogen production and ammonia synthesis
- the POM reaction the H 2 / CO ratio is obtained at about 2
- the individual reforming process includes three types of auto-thermal reforming (ATR) and POM, SRM, and CDR, in which POM and SRM are mixed to increase energy and carbon efficiency while maintaining an appropriate H 2 / CO ratio.
- ATR auto-thermal reforming
- POM and SRM are mixed to increase energy and carbon efficiency while maintaining an appropriate H 2 / CO ratio.
- Tri-reforming and the like, in which reactions are mixed, are well known.
- the present invention is a mixed reforming process, while SRM and CDR are simultaneously processed to produce a synthesis gas using a nickel-based reforming catalyst, and the catalyst system that can be used in the synthesis of methanol and the Fischer-Tropsch reaction process using the same. have.
- the composition ratio of the thermodynamically appropriate syngas (H 2 / (2CO + 3CO 2 )) in methanol synthesis is known to be around 1.05, and as the ratio is increased, the methanol yield increases. To adjust, it is necessary to add additional hydrogen or adjust the conversion in the CDR reaction.
- Ni / Al 2 O 3 catalyst system is mainly used in the range of molar ratio of steam and methane 4 ⁇ 6: 1 at reaction temperature of 750 ⁇ 850 °C, but catalyst deactivation by carbon deposition Due to the severely occurring problems, many studies have been conducted on catalyst systems containing transition metals and alkali metals as precious metals or cocatalysts [Journal of Molecular Catalysis A 147 (1999) 41].
- the catalyst deactivation is more severe than the SRM reaction, and as a method for suppressing the catalyst, a catalyst for the catalyst of the noble metal catalyst (Pt / ZrO 2 ), Ni / MgO, or Ni / MgAlO x series is used.
- a catalyst for the catalyst of the noble metal catalyst Pt / ZrO 2
- Ni / MgO Ni / MgAlO x series
- Many studies have been conducted on catalyst systems containing alkali metals [Catalysis Today 46 (1998) 203, Catalysis communications 2 (2001) 49 and Korean Patent Publication No. 10-2007-0043201).
- CDR + SRM mixed reforming process
- the mixed reforming of methane on the catalyst while suppressing the deactivation of the catalyst by carbon deposition using a catalyst pretreated with a single or two component selected from cerium and zirconium on a MgAlO x metal oxide support using nickel as an active ingredient By using the synthesis gas produced through the reaction (SRM and CDR reforming reaction) to obtain a composition suitable for the methanol synthesis reaction and to introduce the method that can be utilized in the Fischer-Tropsch reaction.
- the Fischer-Tropsch reaction using an iron-based catalyst is excellent for treating syngas having a low H 2 / CO ratio due to its excellent activity for water gas conversion.
- Iron-based catalysts for Fischer-Tropsch synthesis can be prepared by melting or precipitation and also by the spray-drying method, which improves the wear resistance of the catalyst and It is also reported that it does not affect the activity of the catalyst, but merely improves the physical strength of the catalyst [Industrial & Engineering Chemistry Research 40 (2001) 1065].
- iron-based catalysts are prepared that include one or more cocatalysts that aid in the adsorption of CO or the reduction of iron.
- the addition of potassium to the precipitated iron catalyst increases the yield of high molecular weight products and the activity of the catalyst.
- copper can be used as a promoter in Fischer-Tropsch reactions, which generally use iron-based catalysts to promote the reduction of iron.
- Copper is more effective than potassium in the Fischer-Tropsch reaction rate by promoting iron's reducibility, but it reduces the activity of the water gas shift and therefore cannot maintain the appropriate H 2 / CO ratio for Fischer-Tropsch synthesis. There is this.
- the use of copper and metal elements of Groups 1A or 2A as cocatalysts on iron-manganese without a support may be used to selectively synthesize hydrocarbons of C 5+ at high carbon monoxide conversion rates.
- a binder may be used together with a promoter as a structural stabilizer in the iron catalyst system.
- the present invention performs a mixed reforming reaction using a nickel-based reforming catalyst (Ni / Ce (Zr) / MgAlO x ) having excellent catalytic activity as the SRM and CDR reaction proceeds simultaneously as a mixed reforming process, and is produced therefrom.
- a nickel-based reforming catalyst Ni / Ce (Zr) / MgAlO x
- carbon monoxide, carbon dioxide, and hydrogen are produced to maintain the proper composition [H 2 / (2CO + 3CO 2 )], and the synthesis of methanol and Fischer-Tropsch reaction using iron-based catalyst It is intended to be used.
- H suitable for use in methanol synthesis or Fischer-Tropsch reaction 2 / (2CO + 3CO 2 It was found that it is important to select a reaction system that can be prepared in a molar ratio and an appropriate catalyst system.
- the inventors have found that Ni is Ce / MgAlO as a support.
- an object of the present invention is to provide a catalyst for a mixed reforming reaction for a methanol synthesis reaction or a Fischer-Tropsch reaction and a preparation method thereof.
- the present invention has another object to provide a method for producing a synthesis gas using the catalyst.
- the present invention relates to Ce / MgAlO, which is Ni as a support. x or Ce-Zr / MgAlO x It is supported by 5 to 20% by weight, and fired at 600 to 1000 ° C to have a specific surface area of 80 to 200 m 2 / g is a catalyst for mixed reforming reactions.
- MgAlO x Maintaining the content of Ce or Ce-Zr on the support 3 to 20% by weight, and the weight composition ratio (Zr / Ce) of Ce and Zr metal is maintained in the range of 0 to 4 and fired at 600 ⁇ 900 °C Ce (Zr) / MgAlO x Preparing a support for mixing reforming; And 2) Ce / MgAlO as the support, Ni as the active ingredient.
- x or Ce-Zr / MgAlO x It is characterized by a method for producing a catalyst for mixed reforming reaction, characterized in that it comprises 5 to 20% by weight, and calcining at 600 to 1000 °C to prepare a catalyst.
- the catalyst was reduced on the catalyst using hydrogen gas at 700 to 1000 ° C, reaction temperature 800 to 1000 ° C, reaction pressure 0.5 to 20 atmospheres, space velocity 1,000 to 500,000 h -1 , CH 4 / H 2 O
- Method for producing a synthesis gas characterized in that produced under the reaction molar ratio of 1 / 1.0 ⁇ 2.0 / 0.3 ⁇ 0.6 of / CO 2 by a mixed reforming reaction which is carried out at the same time steam reforming reaction of natural gas and carbon dioxide reforming reaction of methane It is another feature.
- the present invention is an economical use of carbon dioxide as a mixed reforming reaction of natural gas and a steam reforming reaction as well as a carbon dioxide reforming reaction of methane to maintain a constant ratio of carbon monoxide, carbon dioxide and hydrogen to synthesis gas suitable for methanol synthesis or A method for producing syngas that can also be utilized in Fischer-Tropsch reactions.
- the present invention also relates to a catalyst system for preparing a synthesis gas on a specific catalyst consisting of Ni / Ce (Zr) / MgAlO x , and performing a methanol synthesis reaction or a Fischer-Tropsch reaction using the same.
- the above catalyst suppresses the inertness of the catalyst due to coke formation during the reaction, and also inhibits the deactivation of the catalyst due to the reoxidation of nickel by water added during the reaction, compared with the catalyst for mixed reforming reactions reported in the prior art. It is characterized by a catalyst having excellent reactivity, a method for producing the same, and a method for producing a synthesis gas using the same.
- Figure 1 shows the XRD pattern after the reaction of the mixed reforming catalyst according to the present invention.
- Figure 2 shows the XRD pattern before the reaction of the mixed reforming catalyst according to the present invention, in the case of the Ni / Ce (Zr) / MgAlO x catalyst used in the example, the particle size change of the nickel before and after the reaction is relatively comparative Compared with the case of using Ni / Ce-Zr / ⁇ -Al 2 O 3 as in the case of 2 was found to be less, it was confirmed that this is associated with the reason that the activity of the catalyst is kept stable.
- the present invention relates to Ce / MgAlO, which is Ni as a support. x or Ce-Zr / MgAlO x It is supported by 5 to 20% by weight, and fired at 600 to 1000 ° C to have a specific surface area of 80 to 200 m 2 It is characterized by a / g mixed reforming reaction catalyst and its preparation method.
- the method for producing a synthesis gas using the catalyst is another feature.
- the present invention is an economical utilization method of carbon dioxide, a mixture reforming that simultaneously performs steam reforming of methane (SRM) of natural gas (CH 4 ) and carbon dioxide reforming of methane (CDR) of methane.
- Synthesis of carbon monoxide, carbon dioxide, and hydrogen as a product to maintain a specific molar ratio (H 2 / (2CO + 3CO 2 ) 0.85 to 1.15) to facilitate methanol synthesis or Fischer-Tropsch reaction
- a reforming catalyst named Ni / Ce (Zr) / MgAlO x ) for producing a gas.
- a catalyst system which minimizes the production of by-products disclosed in the prior patent (Korean Patent Application No. 2008-0072286) and a conventional commercial Cu-ZnO-Al 2 O 3 catalyst may be used.
- the SRM and CDR reactions have an equilibrium conversion rate depending on the ratio of reactants CH 4 / CO 2 / water vapor, reaction pressure and reaction temperature, and the conversion rate of CDR reactions decreases with increasing reaction pressure. Speed also increases.
- the initial investment cost is reduced by reducing the size of the reactor, and in order to reduce the cost of the separation process, the reforming reaction is usually performed at a reaction pressure of 1.0 MPa or more.
- the mixed reforming reaction it is advantageous to minimize the use of water vapor because the conversion rate of CO 2 decreases as the amount of water vapor in the feed composition increases with the reaction pressure, but this affects the lifetime of the catalyst due to carbon deposition. It is necessary to develop a catalyst that suppresses deactivation even under the condition of.
- the carbon monoxide, carbon dioxide, and hydrogen are in a certain ratio [H 2 / () by the mixed reforming reaction which satisfies the above conditions and suppresses the deactivation of the catalyst to perform steam reforming of natural gas and carbon dioxide reforming of methane.
- 2CO + 3CO 2 ) 0.85 ⁇ 1.15]
- Ni / Ce (Zr) / MgAlO x to prepare a synthesis gas suitable for methanol synthesis or Fischer-Tropsch reaction as an economical use of carbon dioxide It is about the specific catalyst which consists of.
- H 2 / (2CO + 3CO 2 ) 0.85 to 1.15 as a mixed reforming reaction in which steam reforming of natural gas and carbon dioxide reforming of methane are simultaneously performed on a catalyst composed of Ni / Ce (Zr) / MgAlO x .
- the reaction conditions are introduced to show excellent activity in methanol synthesis reaction and Fischer-Tropsch reaction.
- the mixed reforming reaction consists of steam reforming of methane (SRM) of natural gas (CH 4 ) and carbon dioxide reforming of methane (CDR).
- SRM steam reforming of methane
- CDR carbon dioxide reforming of methane
- the mole ratio of H 2 / (2CO + 3CO 2 ) is 0.85 to 1.15. If the H 2 / (2CO + 3CO 2 ) molar ratio is less than 0.85 there is a problem that the one-time conversion rate of carbon monoxide and carbon dioxide is reduced due to the lack of hydrogen, when the excess of 1.15 molar ratio is excessive recycling of unreacted hydrogen It is advisable to maintain this range because problems may occur that reduce the efficiency of the process.
- the catalyst used in the mixed reforming reaction uses a specific catalyst consisting of Ni-Ce (Zr) / MgAlO x to maintain a constant H 2 / (2CO + 3CO 2 ) molar ratio during the reaction due to inhibition of inactivation by carbon deposition.
- MgAlO x having a hydrotalcite structure which is used as a support for a mixed reforming reaction, may be prepared by using the following coprecipitation method or commercially available Mg 2 AlO 4 (PURAL MG series, SASOL).
- MgAlO x supports prepared by coprecipitation are generally used in the art and have a specific surface area of 100 to 400 m 2 / g, preferably 150 to 300 m 2 / g and a MgO / Al 2 O 3 molar ratio in the range of 0.2 to 0.8. It can be used to satisfy.
- the specific surface area of MgAlO x is less than 100 m 2 / g, the specific surface area of the support is small, causing a problem of decreasing the dispersibility of the active ingredient, thereby reducing the activity of the catalyst, and using a support of more than 400 m 2 / g There is a problem that the thermal stability of the support is reduced to reduce the activity of the catalyst due to the sintering phenomenon of the support during the catalyst preparation and reaction process.
- the MgO / Al 2 O 3 molar ratio is 0.2 or less, the phenomenon similar to the case of using Ni / Al 2 O 3 , which is a conventional commercialization catalyst, is reduced and the activity of the catalyst due to nickel aluminate formation during the mixing reforming reaction is reduced. This may occur, and if it exceeds 0.8, the hydrotalcite structure generated during the high temperature firing process may not be stabilized, and thus the catalyst may be deactivated, thereby maintaining the above range.
- a basic precipitant is added to a metal mixture of an alumina precursor and a magnesium precursor, followed by introducing a process of filtering and washing the precipitate formed by coprecipitation and aging under a basic aqueous solution of pH 10.
- the metal mixture of the alumina precursor and the magnesium precursor may specifically use acetate salt, hydroxide salt or nitrate as a precursor of each metal generally used in the art.
- the basic precipitant is generally used in the art, and specifically, sodium carbonate (Na 2 CO 3 ), potassium carbonate (K 2 CO 3 ), ammonium carbonate ((NH 4 ) 2 CO 3 ) or sodium hydrogencarbonate (NaHCO 3 ) And the like are preferable.
- the catalyst is aged to prepare a precipitate.
- the aging is appropriately maintained at 50 to 90 °C for 2 to 20 hours or more, preferably 2 to 15 hours, which is suitable for the specific surface area and stabilized hydrotalcite structure of MgAlO x of the appropriate size in the aging time range.
- the formation of oxides is advantageous. If the aging temperature is less than 50 °C in the aging process, there is a disadvantage in that the formation of the structure of the MgAlO x oxide is difficult, and if it exceeds 90 °C, the particle size of the MgAlO x oxide support is increased to reduce the specific surface area.
- the aging time is less than 2 hours, the structure of the MgAlO x oxide is not well developed, and if it exceeds 20 hours, the particle size of the MgAlO x oxide support is increased to decrease the active point of the final catalyst due to the reduction of specific surface area.
- the increase in synthesis time is not economical and therefore not appropriate.
- the precipitate is dried in an oven at 100 ° C. or higher, specifically 100 to 150 ° C. for at least one day, and then calcined at 500 to 1000 ° C., preferably 600 to 900 ° C. to prepare a catalyst. After drying, the calcination process can be omitted and used directly for catalyst preparation. If the firing temperature is less than 500 °C metal precursor is not converted to the oxide form does not form a suitable structure there is a problem that the specific surface area of the support is reduced, if the temperature exceeds 1000 °C due to the growth of the particle size of the support The reduction of the surface area leads to the problem that the dispersibility of the active ingredient is reduced and the reaction rate of the mixing modification is reduced.
- the activity of the mixed reforming reaction may be increased by increasing the dispersibility of the catalyst particles in the process of supporting the active ingredient, but MgAlO x having a hydrotalcite structure is appropriate.
- the problem may arise due to the inability to convert to the oxide form of the structure, thus making the preparation of the MgAlO x support prepared in the equivalence ratio for the formation of the spinel structure important.
- a method for preparing a catalyst for mixed reforming reaction is prepared by the following impregnation method.
- a Ce component known to have an oxygen storage capacity or an acid point and a base point are simultaneously introduced to include a Ce-Zr component that can suppress carbon deposition.
- MgAlO x is pretreated with a support. The pretreatment method is based on the results of the previous research of the research team (Korean Patent Publication No. 2002-0021721, Korean Patent Publication No. 2004-0051953 and Korean Patent Publication No. 2002-0088213), and the zirconia component modified with cerium is used. In the case of use, it was reported that the deactivation of the catalyst by carbon deposition can be suppressed.
- the content of Ce or Ce-Zr in the component consisting of Ce (Zr) / MgAlO x in the method for preparing a support for a mixed reforming catalyst used is prepared by maintaining 3 to 20% by weight relative to the weight of MgAlO x.
- the Ce or Ce-Zr content is less than 3% by weight, the effect of inhibiting carbon deposition by the pretreatment is insignificant, and when it exceeds 20% by weight, Ni is reduced due to the specific surface area due to the pore blockage of the support MgAlO x .
- the activity of the catalyst is reduced due to the decrease in the dispersibility of
- the weight composition ratio (Zr / Ce) of Ce and Zr metals which are the pretreatment components of the MgAlO x support, is maintained in the range of 0 to 4.
- the active ingredient Since the dispersibility of phosphorus Ni may decrease and the activity may decrease, there is a need to maintain the above range.
- the Ce and Zr precursors may be specifically used as a precursor of each metal commonly used in the art, such as acetate salts, hydroxide salts or nitrates, more specifically, after supporting the Ce and Zr precursor on the MgAlO x support , And dried at 100 to 200 ° C. and calcined at 600 to 1000 ° C., preferably 700 to 900 ° C.
- the impregnation method is carried out in an aqueous solution or an alcohol solution at a temperature in the range of 40 ⁇ 90 °C, the product prepared in the above process is removed from the solvent using a vacuum dryer for evaporation of the solvent in about 100 °C or more in the oven After drying for 24 hours, it is calcined and used as a catalyst.
- the support of the mixed reforming reaction prepared by the above method additionally supports Ni as an active ingredient in an amount of 5 to 20 wt% based on Ce (Zr) / MgAlO x as the support to prepare a final catalyst.
- the precursor of the nickel metal to be used may be specifically used acetate salt, hydroxide salt or nitrate, and more specifically, after supporting the nickel precursor on the Ce (Zr) / MgAlO x support, at 100 ⁇ 200 °C Dry and fire in the range 600-1000 degreeC, Preferably it is 700-900 degreeC.
- the specific surface area of the Ni / Ce (Zr) / MgAlO x catalyst prepared by the above method is to be prepared in the range of 80 to 200 m 2 / g.
- the content of nickel supported by the active ingredient is less than 5% by weight, the content of nickel which is active in the reforming reaction is small and the activity is decreased.
- the support of Ce (Zr) / MgAlO x as a support It may be necessary to maintain the above range because pore blocking may reduce the dispersibility of nickel and decrease the activity of the catalyst.
- a MgAlO x catalyst is Ni and Ce and at least one member selected from Zr metal for the precursor at the same time supported on the MgAlO x support Ni / Ce (Zr) / MgAlO x It is a method of preparing a catalyst. More specifically, the MgAlO x support is supported on at least one metal compound selected from Ni, Ce, and Zr precursors, and then dried at 100 to 200 ° C., preferably at 600 to 1000 ° C., preferably at 700 to 900 ° C. By firing, the specific surface area of the Ni / Ce (Zr) / MgAlO x catalyst is prepared in the range of 80 to 200 m 2 / g.
- the present inventors have confirmed that the yield of methanol is improved in the composition of the synthesis gas containing CO 2 rather than the composition gas containing only CO and H 2 coexist, and CO / (CO + When the molar ratio of CO 2 ) is 0.6 ⁇ 0.8, it was confirmed that the yield of methanol is the maximum.
- the molar ratio of 2 is in the range of 1 / 1.0 to 2.0 / 0.3 to 0.6, the reaction temperature 800 to 1000 °C and the reaction pressure 0.5 to 20 atm, the need to maintain the conversion rate of more than 80% of methane and 45% or more of carbon dioxide There is this.
- the catalyst proposed in the present invention for 20 hours H 2 / (2CO + 3CO 2 ) proposed a catalyst which is a change in the molar ratio of the active is maintained at less than 2%.
- the pressure of the mixed reforming reaction can be operated from atmospheric pressure to 20 atm, and in the case of low pressure, the equilibrium conversion rate is increased, but the reactor volume is increased, the initial investment is increased, and the economical efficiency is reduced by using a high pressure booster for separation of the product.
- the equilibrium conversion rate of methane and carbon dioxide decreases along with an increase in the deactivation rate of the catalyst.
- the molar ratio of CH 4 / H 2 O / CO 2 which is a reforming reactant, is 1 / 1.0 to 2.0 / 0.3 in order to maintain an optimal feed condition for the methanol synthesis reaction, H 2 / (2CO + 3CO 2 ) molar ratio 0.85 to 1.15.
- the reduction in CO 2 utilization conversion rate is reduced in the CO 2 by the carbon deposition if 0.6, there is a need to maintain a range of not more than a molar ratio of methane compared to H 2 O 1.0 There is a problem.
- the catalyst for the mixed reforming reaction presented above is used after the reduction treatment in the temperature range of 700 to 1,000 ° C. before the reforming reaction.
- the mixing reforming reaction is carried out at a reaction temperature of 800 to 1,000 ° C., a reaction pressure of 0.5 to 20 atm, and a space velocity condition of 1,000 to 500,000 h ⁇ 1 .
- the conversion rate of CH 4 obtained after the activity of the catalyst is stabilized by the mixed reforming reaction is 80% or more, and the conversion rate of CO 2 is 45% or more.
- PURAL MG30 a MgAlO x (30) support having a hydrotalcite structure having a MgO / Al 2 O 3 ratio of 3/7, as a catalyst support for mixed reforming reaction (manufactured by sasol, with a specific surface area of at least 250 m 2 / g)
- the Ce metal is 4% by weight with respect to the MgAlO x (30) support by using cerium acetate by impregnation method, and at the same time using nickel nitrate (Ni (NO 3 ) 2 .6H 2 O) as a nickel precursor.
- Ni (NO 3 ) 2 .6H 2 O) nickel nitrate
- the specific surface area of the prepared catalyst was 117 m 2 / g, the pore volume was 0.34 cc / g and the average pore size was 12.4 nm.
- a catalyst was prepared in the same manner as in Example 1, except that PURAL MG50 (manufactured by Sasol, a specific surface area of at least 200 m 2 , having a MgAlO x (50) support having a hydrotalcite structure having a MgO / Al 2 O 3 ratio of 5/5). / g or more) to prepare the final catalyst Ni / Ce / MgAlO x (50).
- the specific surface area of the catalyst was 117 m 2 / g, the pore volume was 0.30 cc / g and the average pore size was 13.2 nm.
- a catalyst was prepared in the same manner as in Example 1, except that PURAL MG70 (manufactured by Sasol, a specific surface area of at least 180 m 2 , having a MgAlO x (70) support having a hydrotalcite structure having a MgO / Al 2 O 3 ratio of 7/3) / g or more) to prepare Ni / Ce / MgAlO x (70) as the final catalyst.
- the specific surface area of the catalyst was 104 m 2 / g, the pore volume was 0.24 cc / g, and the average pore size was 11.0 nm.
- MgO / Al 2 O 3 MgAlO of hydrotalcite structure with ratio 3/7 x (30) PURAL MG30 as a support manufactured by sasol, with a specific surface area of at least 250 m 2 / g or more
- MgAlO x (30) Zr / Ce using cerium acetate and zirconium nitrate by impregnation with respect to the support The ratio is 0.25 by weight
- Ni (NO 3 ) 2 6H 2 Ce-Zr / MgAlO using O) x After carrying 15% by weight of nickel supported on the support and stirring for 12 hours at 70 °C using a vacuum dryer after removing water as a solvent, dried at 100 °C oven
- Ce-Zr / MgAlO x (30) A support was prepared. The support was prepared by supporting 12 wt% of nickel and stirring at 70 ° C. for 12 hours, then removing water as a solvent, drying at 100 ° C. for at least 24 hours, and then calcining at 550 ° C. for 6 hours to obtain Ni as a final catalyst. / Ce-Zr / MgAlO x (30) was prepared. At this time, the specific surface area of the catalyst is 96 m 2 / g, pore volume was 0.31 cc / g and average pore size was 16.5 nm.
- a catalyst was prepared in the same manner as in Example 1, except that PURAL MG30 (manufactured by Sasol, a specific surface area of 250 m 2 , having a MgAlO x (30) support having a hydrotalcite structure having a MgO / Al 2 O 3 ratio of 3/7) / g or more) and only nickel was supported at 12% by weight relative to the support to prepare a Ni / MgAlO x (30) catalyst.
- the specific surface area of the catalyst was 118 m 2 / g
- the pore volume was 0.34 cc / g
- the average pore size was 13.8 nm.
- Example 4 To prepare a catalyst in the same manner as in Example 4, the specific surface area 200 m 2 Zr / Ce using cerium acetate and zirconium nitrate by impregnation using gamma-alumina from SASOl The ratio was 0.75 by weight, and supported by 5% by weight relative to the alumina support, followed by drying and firing at 900 ° C. for 6 hours to produce Ce-Zr / ⁇ -Al. 2 O 3 The support was prepared.
- Ni / Ce-Zr / ⁇ -Al 2 O 3 was prepared.
- the specific surface area of the catalyst is 110 m 2 / g
- pore volume was 0.34 cc / g
- average pore size was 14.1 nm.
- Example 1 Ni / Ce / MgAlO x (30) 86/59 84/58 0.87 0.86 -1.15
- Example 2 Ni / Ce / MgAlO x (50) 85/55 84/59 0.87 0.86 -1.15
- Example 3 Ni / Ce / MgAlO x (70) 80/45 80/45 0.85 0.85 0.00
- Example 4 Ni-Ce-Zr / MgAlO x (30) 84/58 83/56 0.86 0.86 0.00
- Example 5 Ni / Ce-Zr / MgAlO x (30) 86/56 85/57 0.87 0.87 0.00 Comparative Example 1 Ni / MgAlO x (30) 86/56 85/57 0.87 0.87 0.00 Comparative Example 1 Ni / MgAlO x (30) 86/56 85/57 0.87 0.87 0.00 Comparative Example 1 Ni / MgAlO x (30) 86/56 85/57 0.87
- a synthetic gas is prepared through a mixed reforming reaction which simultaneously performs a carbon dioxide reforming reaction (CDR) of methane and a steam reforming reaction (SRM) of methane as an economic utilization method of carbon dioxide, and utilizes the synthesis or fisher- A catalyst has been developed that can improve the long-term performance stability of the reforming catalyst for application to the Tropsch reaction.
- CDR carbon dioxide reforming reaction
- SRM steam reforming reaction
- methanol produced primarily may be an inducer capable of producing various derivatives such as DME, DMC, biodiesel and synthetic gasoline, and hydrocarbons generated by the Fischer-Tropsch reaction may also be used as various chemical raw materials.
- the reforming catalyst system proposed in the present invention may greatly contribute to the development of a process for economically utilizing carbon dioxide.
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Abstract
Description
구분 | 촉매 조성 | CH4 전환율/CO2 전환율(카본 몰%) | H2/(2CO+3CO2) 몰비 | H2/(2CO+3CO2) 몰비 변화(%) a | ||
반응 3시간 후 | 반응 20시간 후 | 반응 3시간 후 | 반응 20시간 후 | |||
실시예 1 | Ni/Ce/MgAlOx (30) | 86 / 59 | 84 / 58 | 0.87 | 0.86 | - 1.15 |
실시예 2 | Ni/Ce/MgAlOx (50) | 85 / 55 | 84 / 59 | 0.87 | 0.86 | - 1.15 |
실시예 3 | Ni/Ce/MgAlOx (70) | 80 / 45 | 80 / 45 | 0.85 | 0.85 | 0.00 |
실시예 4 | Ni-Ce-Zr/MgAlOx (30) | 84 / 58 | 83 / 56 | 0.86 | 0.86 | 0.00 |
실시예 5 | Ni/Ce-Zr/MgAlOx (30) | 86 / 56 | 85 / 57 | 0.87 | 0.87 | 0.00 |
비교예 1 | Ni/MgAlOx (30) | 81 / 48 | 80 / 42 | 0.85 | 0.83 | - 2.35 |
비교예 2 | Ni/Ce-Zr/γ-Al2O3 | 73 / 46 | 77 / 52 | 0.81 | 0.83 | + 2.47 |
a H2/(2CO+3CO2) 몰비의 변화는 반응 3시간 후와 20시간 후의 변화 비율을 퍼센트 단위로 나타냄 |
구 분 | 촉매 조성 | NiO 및 Ni 입자 크기 (nm) | 입자 크기증가도(%) a | |
반응 전 (NiO, 2θ = 37.2o) | 반응 후 (Ni, 2θ = 44.5o) | |||
실시예 1 | Ni/Ce/MgAlOx (30) | 11.3 | 16.4 | + 45.1 |
실시예 2 | Ni/Ce/MgAlOx (50) | 12.4 | 24.1 | + 94.4 |
실시예 3 | Ni/Ce/MgAlOx (70) | 14.7 | 28.6 | + 94.6 |
실시예 4 | Ni-Ce-Zr/MgAlOx (30) | 11.5 | 24.0 | + 108.7 |
실시예 5 | Ni/Ce-Zr/MgAlOx (30) | 11.7 | 16.6 | + 41.9 |
비교예 1 | Ni/MgAlOx (30) | 11.8 | 18.0 | + 52.5 |
비교예 2 | Ni/Ce-Zr/γ-Al2O3 | 14.3 | 35.2 | + 146.2 |
a 니켈 입자 크기 증가도는 반응 전 NiO 입자 크기와 반응 후의 Ni 입자 크기의 비로 퍼센트 단위임.입자 크기 증가도(%)=(Ni 입자 크기 - NiO 입자 크기)/NiO 입자 크기*100 |
Claims (11)
- 활성 성분으로서 Ni를 지지체인 Ce/MgAlOx 또는 Ce-Zr/MgAlOx 대비 5 ~ 20 중량%로 담지하고, 600 ∼ 1000 ℃에서 소성하여 비표면적이 80 ~ 200 m2/g인 것을 특징으로 하는 혼합 개질 반응용 촉매.
- 제 1 항에 있어서,상기 촉매는 메탄올 합성 반응 또는 피셔-트롭쉬 반응을 위한 합성가스 제조에 사용되는 것을 특징으로 하는 혼합 개질 반응용 촉매.
- 1) MgAlOx 지지체 상에 Ce 또는 Ce-Zr의 함량을 3 ~ 20 중량%를 유지하고, Ce과 Zr 금속의 중량 조성비(Zr/Ce)는 0 ~ 4의 범위를 유지하게 하여 600 ∼ 900 ℃에서 소성시켜 Ce(Zr)/MgAlOx 혼합 개질용 지지체를 제조하는 단계; 및2) 활성 성분으로서 Ni를 지지체인 Ce/MgAlOx 또는 Ce-Zr/MgAlOx 대비 5 ~ 20 중량%로 담지하고, 600 ∼ 1000 ℃에서 소성하여 촉매를 제조하는 단계를 포함하여 이루어진 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- 제 3 항에 있어서,상기 MgAlOx 지지체는 알루미나 전구체와 마그네슘 전구체의 금속 혼합물에 염기성 침전제를 가하여 염기성 수용액 하에서 공침하여 제조된 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- 제 4 항에 있어서,상기 알루미나 전구체 또는 마그네슘 전구체는 아세테이트염, 수산화염 또는 질산염인 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- 제 4 항에 있어서,상기 염기성 침전제는 탄산나트륨(Na2CO3), 탄산칼륨(K2CO3), 탄산암모늄((NH4)2CO3) 또는 탄산수소나트륨(NaHCO3)인 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- MgAlOx 지지체 상에 사용되는 금속 전구체인 Ni와 함께 Ce 또는 Ce-Zr를 동시에 담지시켜 600 ∼ 1000 ℃에서 소성하여 촉매를 제조하는 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- 제 7 항에 있어서,상기 금속 전구체는 아세테이트염, 수산화염 및 질산염 중에서 선택된 1종 이상인 것을 특징으로 하는 혼합 개질 반응용 촉매 제조방법.
- 제 1 항 또는 제 2 항의 촉매를 700 ~ 1000 ℃에서 수소 기체를 이용하여 환원 처리한 촉매 상에서, 반응 온도 800 ~ 1000 ℃, 반응 압력 0.5 ~ 20 기압, 공간 속도 1,000 ~ 500,000 h-1, CH4/H2O/CO2의 반응 몰비 1/1.0 ~ 2.0/0.3 ~ 0.6의 조건 하에서, 천연가스의 수증기 개질 반응과 메탄의 이산화탄소 개질 반응이 동시에 수행되는 혼합 개질 반응으로 제조하는 것을 특징으로 하는 합성가스 제조방법.
- 제 9 항에 있어서,상기 혼합 개질 반응은 CH4의 전환율이 80% 이상이며, CO2의 전환율이 45% 이상을 유지하고, H2/(2CO+3CO2) 몰비가 0.85 ~ 1.15를 유지하는 것을 특징으로 하는 합성가스 제조방법.
- 제 9 항에 있어서,상기 혼합 개질 반응의 운전 조건에서 H2/(2CO+3CO2) 몰비의 변화가 2% 미만인 것을 특징으로 하는 합성가스 제조방법.
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CN112844397B (zh) * | 2021-01-22 | 2023-02-10 | 成都理工大学 | 一种用于乙酸自热重整制氢的铈钐固溶体镍基催化剂 |
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AU2009277275A1 (en) | 2010-02-04 |
EP2308594A4 (en) | 2012-11-21 |
KR20100014012A (ko) | 2010-02-10 |
WO2010013958A3 (ko) | 2010-06-10 |
US8524119B2 (en) | 2013-09-03 |
US20110114892A1 (en) | 2011-05-19 |
CN102112227B (zh) | 2015-05-20 |
CN102112227A (zh) | 2011-06-29 |
AU2009277275B2 (en) | 2012-12-13 |
EP2308594A2 (en) | 2011-04-13 |
KR100991263B1 (ko) | 2010-11-01 |
JP2011529394A (ja) | 2011-12-08 |
JP5285776B2 (ja) | 2013-09-11 |
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