CN103977801B - A kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst and method for making and application - Google Patents
A kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst and method for making and application Download PDFInfo
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Abstract
A kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst is made up of active component and carrier, and its percentage by weight consists of cobalt oxide: 5-35%, and all the other are metallic carrier.The present invention, by adopting metal powder as catalyst carrier, drastically increases the heat transfer efficiency of beds, effectively prevent the generation emerging " temperature runaway " of fixed bed " focus ".
Description
Technical field
The present invention relates to a kind of catalyst and preparation method and application, is a kind of high thermal conductive metallic load cobalt catalyst and preparation method and the application in F-T synthesis specifically.
Technical background
F-T synthesis refers to process coal, natural gas or living beings being converted under catalyst action hydro carbons through synthesis gas.The catalyst of the industrial employing of F-T synthesis is divided into iron-based and cobalt-based two class, and wherein cobalt-base catalyst has active high, and methane selectively is low, C
5+selective height and the low advantage of water gas reaction and become the catalyst of most competitive superiority in F-T synthesis.Therefore design high-performance, the Co based Fischer-Tropsch synthesis catalyst of low price has great importance.
Co-based fischer-tropsch synthesis reactor mainly contains paste state bed reactor and fixed bed reactors.Wherein fixed bed reactors have easy and simple to handle, the segregative advantage of product.But due to the high exothermic character of fischer-tropsch reaction, be easy to form " focus " in course of reaction in fixed bed bed, even cause time serious " temperature runaway ".In order to overcome this problem, shell company has carried out many transformations with enhanced reactor internal heat transfer to constructing in reactor, but which results in the increase of reactor design and processing charges.US2011135543 discloses a kind of MFEC technique of augmentation of heat transfer.Adopt micro-sized metal fiber to be matrix, above catalyst granules is attached to, utilize the high thermal conduction characteristic of metallic fiber, increase the heat conductivility of bed.But this technology has behaviour does complexity, and catalyst utilization is low, catalyst granules such as easily to run off at the shortcoming.
Summary of the invention
The object of this invention is to provide a kind of Metal Supported Co catalysts of high thermal conductivity and preparation method and the application in F-T synthesis.
Metal material has high heat conductivility, simultaneously there is the complete nanoscale film of one deck at some metal material surface, and this oxide-film at high temperature can stable existence, avoids interior metal to be oxidized.Based on above characteristic, metal material is as co-based fischer-tropsch catalyst carrier, and the heat transfer efficiency of its high thermal conduction characteristic energy fortifying catalytic agent bed, avoids bed " focus " to be emerged; Oxide-film energy " grappling " active component on surface, promotes the dispersion of active component simultaneously; Metal material also has its cheap market price, the sufficient advantage of raw material sources in addition.Therefore prepare Co based Fischer-Tropsch synthesis catalyst using metal material as carrier and there is greatly actual application value and great commercial promise.
Catalyst of the present invention is made up of active component and carrier, and its percentage by weight consists of: cobalt oxide: 5-35%, and all the other are metallic carrier.
Metallic carrier as above is magnesium powder, copper powder, aluminium powder, zinc powder, iron powder, magnesium aluminum-alloy powder or SiCuAl alloyed powder.
Metallic carrier average grain scope 10 ~ 50 μm as above, specific surface is 70 ~ 650m
2/ g, mesoporous pore size 2 ~ 30nm, macropore diameter 50 ~ 90nm, pore volume is 0.25 ~ 3.00cm
3/ g.
The preparation method of catalyst of the present invention is as follows:
(1) be that the metal powder of 10 ~ 50 μm is put into distilled water and boiled 6 ~ 10h by particle diameter, filter, by filter cake dry 10 ~ 20h at 60 ~ 100 DEG C;
(2) 1.0 × 10 are configured
-6~ 1.0 × 10
-2mol/L acid or aqueous slkali;
(3) when metal powder is aluminium powder, magnesium aluminum-alloy powder or SiCuAl alloyed powder, by metal powder: acid or aqueous slkali=5g:2-5L, the metal powder of step (1) is joined in the solution of step (2), and after electromagnetic agitation process 10 ~ 30h, filter, washing is to neutral, and filter cake is dry 10 ~ 30h at 60 ~ 100 DEG C;
When metal powder is magnesium, copper, iron or zinc, by metal powder: acid solution=5g:2-5L, the metal powder of step (1) is joined in the solution of step (2), and after electromagnetic agitation process 10 ~ 30h, filter, washing is to neutral, and filter cake is dry 10 ~ 30h at 60 ~ 100 DEG C;
(4) by the material of step (3) gained roasting 6 ~ 10h under 300 ~ 600 DEG C of nitrogen atmospheres, metal powder carrier is obtained.
(5) equi-volume impregnating is adopted, soluble cobalt is dissolved in deionized water, flood with step (4) gained metallic carrier at ambient temperature, dip time is 6 ~ 10h, after dipping at 60 ~ 100 DEG C dry 10 ~ 20h, carry out roasting under nitrogen atmosphere after dry, sintering temperature is 200 ~ 400 DEG C, and roasting time is 3 ~ 8h.
Acid as above is acetic acid, nitric acid or hydrochloric acid, and alkali is potassium hydroxide or NaOH.
Cobalt salt as above is cobalt nitrate or cobalt acetate.
The catalyst specific surface that the present invention obtains is 50 ~ 600m
2/ g.
The application process of catalyst of the present invention is as follows:
(1) catalyst reduces in fixed bed reactors in the hydrogen of 300 ~ 600 DEG C, and reducing gas volume space velocity is 500 ~ 2000h
-1, reduction pressure is 0.1 ~ 1.0Mpa, and the recovery time is 5 ~ 20h.
(2) reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is between 1 ~ 3, and reaction temperature is 190 DEG C ~ 240 DEG C, and pressure is 1.0 ~ 3.0Mpa, and volume space velocity is 500 ~ 2000h
-1.
The present invention compared with prior art tool has the following advantages:
1, conventional cellular woven wire integrated catalyst carrier, voidage is too high, aperture is excessive (grade), causes fixed bed reactors utilization rate low; The coat on top layer easily departs from the reaction, causes loss of active component.And catalyst prepared by the present invention, reactor utilization ratio is high, and active component not easily runs off.
2, by adopting metal powder as catalyst carrier, drastically increasing the heat transfer efficiency of beds, effectively prevent the generation emerging " temperature runaway " of fixed bed " focus ".
3, catalyst preparation process is simple, cheap.
Detailed description of the invention
The present invention will be further described for embodiment below, and protection scope of the present invention is not by the restriction of these embodiments.
Embodiment 1:
Catalyst preparing: metallic aluminium powder (particle diameter 10 ~ 15 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-6in mol/L sodium hydroxide solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier, carrier specific surface is 72m
2/ g, mesoporous pore size 4nm, macropore diameter 52nm, pore volume is 0.26cm
3/ g.15 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained: cobalt oxide 15%, all the other are metallic aluminium powder carrier.Catalyst specific surface is 50m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h-
1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 220 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1000h
-1.Reaction result is in table 1.
Embodiment 2:
Catalyst preparing: copper powder (particle diameter 40 ~ 45 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-5in mol/L salpeter solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier specific surface is 98m
2/ g, mesoporous pore size 8nm, macropore diameter 55nm, pore volume is 0.41cm
3/ g.15 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained is: cobalt oxide 15%, and all the other are copper powder carrier.Catalyst specific surface is 125m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 220 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1000h
-1.Reaction result is in table 2.
Embodiment 3:
Catalyst preparing: metal magnesium powder (particle diameter 25 ~ 30 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-3in mol/L acetic acid solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier specific surface is 190m
2/ g, mesoporous pore size 6nm, macropore diameter 60nm, pore volume is 0.9cm
3/ g.15 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained is: cobalt oxide 15%, and all the other are metal magnesium powder carrier.Catalyst specific surface is 416m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 220 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1000h
-1.Reaction result is in table 3.
Embodiment 4:
Catalyst preparing: SiCuAl alloy (mass percent Si12%Cu2%Al86%, particle diameter 30 ~ 35 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-2in mol/L hydrochloric acid solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier specific surface is 320m
2/ g, mesoporous pore size 5nm, macropore diameter 53nm, pore volume is 1.25cm
3/ g.15 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained is: cobalt oxide 15%, and all the other are SiCuAl alloyed powder carrier.Catalyst specific surface is 599m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 230 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1500h
-1.Reaction result is in table 4.
Embodiment 5:
Catalyst preparing: metallic aluminium powder (particle diameter 45 ~ 50 μm) is put into distilled water and boiled 6h, to filter, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-3in mol/L acetic acid solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier specific surface is 190m
2/ g, mesoporous pore size 6nm, macropore diameter 60nm, pore volume is 0.9cm
3/ g.30 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained: cobalt oxide 30%, all the other are metallic aluminium powder carrier.Catalyst specific surface is 398m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 200 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1500h
-1.Reaction result is in table 5.
Embodiment 6:
Catalyst preparing: MgAl alloyed powder (mass percent Mg5%Al95%, particle diameter 10 ~ 15 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-2in mol/L potassium hydroxide solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier vector specific surface is 430m
2/ g, mesoporous pore size 12nm, macropore diameter 60nm, pore volume is 1.6cm
3/ g.30 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained is: cobalt oxide 30%, and all the other are MgAl alloyed powder carrier.Catalyst specific surface is 586m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 240 DEG C, and pressure is 2.0Mpa, and volume space velocity is 2000h
-1.Reaction result is in table 6.
Embodiment 7:
Catalyst preparing: MgAl alloyed powder (mass percent Mg5%Al95%, particle diameter 15 ~ 20 μm) is put into distilled water and boils 6h, filters, by filter cake dry 20h at 60 DEG C.Gained material is joined 2L1.0 × 10
-3in mol/L salpeter solution, after electromagnetic agitation process 10h, filter, washing is to neutral, and filter cake is dry 10h at 60 DEG C, and 300 DEG C of roasting 6h in a nitrogen atmosphere after drying, obtain catalyst carrier.Carrier specific surface is 260m
2/ g, mesoporous pore size 13nm, macropore diameter 65nm, pore volume is 1.1cm
3/ g.30 (wt) % accounting for final catalyst by cobalt oxide takes Co (NO
3)
26H
2o, measures deionized water according to equi-volume impregnating, and configuration salting liquid also impregnated in above-mentioned carrier, and dip time is 6h, after dipping at 60 DEG C dry 10h, carry out roasting in a nitrogen atmosphere after drying, sintering temperature is 300 DEG C, and roasting time is 4h.The catalyst weight percent obtained: cobalt oxide 30%, all the other are MgAl alloyed powder carrier.Catalyst specific surface is 150m
2/ g.
In fixed bed reactors, (Ф 10 × 500mm) does not dilute the above-mentioned catalyst of filling 2ml, and reduce in the hydrogen of 400 DEG C, reducing gas volume space velocity is 1500h
-1, reduction pressure is 1.0Mpa, and the recovery time is 5h.Reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is 2, and reaction temperature is 210 DEG C, and pressure is 2.0Mpa, and volume space velocity is 1500h
-1.Reaction result is in table 7.
Table 1 Catalyst Testing Conditions and reaction result
| Catalyst | Reaction condition | CO conversion ratio % | C 1Selective % | C 5+Selective % |
| Embodiment 1 | 220℃,1000h -1 | 31.2 | 7.2 | 85.3 |
| Embodiment 2 | 220℃,1000h -1 | 38.9 | 6.8 | 86.4 |
| Embodiment 3 | 220℃,1000h -1 | 45.2 | 6.6 | 88.2 |
| Embodiment 4 | 230℃,1500h -1 | 56.3 | 8.6 | 84.9 |
| Embodiment 5 | 200℃,1500h -1 | 53.2 | 5.8 | 91.2 |
| Embodiment 6 | 240℃,2000h -1 | 71.2 | 9.6 | 83.7 |
| Embodiment 7 | 210℃,1500h -1 | 67.9 | 6.2 | 87.9 |
Claims (8)
1. a high-termal conductivity Co based Fischer-Tropsch synthesis catalyst, it is characterized in that catalyst is made up of active component and carrier, its percentage by weight consists of active component cobalt oxide: 5-35%, and all the other are metal powder carrier;
And prepared by following steps:
(1) be that the metal powder of 10 ~ 50 μm is put into distilled water and boiled 6 ~ 10h by particle diameter, filter, by filter cake dry 10 ~ 20h at 60 ~ 100 DEG C;
(2) 1.0 × 10 are configured
-6~ 1.0 × 10
-2mol/L acid or aqueous slkali;
(3) when metal powder is aluminium powder, magnesium aluminum-alloy powder or SiCuAl alloyed powder, by metal powder: acid or aqueous slkali=5g:2-5L, the metal powder of step (1) is joined in the solution of step (2), and after electromagnetic agitation process 10 ~ 30h, filter, washing is to neutral, and filter cake is dry 10 ~ 30h at 60 ~ 100 DEG C;
When metal powder is magnesium powder, copper powder, iron powder or zinc powder, by metal powder: acid solution=5g:2-5L, the metal powder of step (1) is joined in the solution of step (2), and after electromagnetic agitation process 10 ~ 30h, filter, washing is to neutral, and filter cake is dry 10 ~ 30h at 60 ~ 100 DEG C;
(4) by the material of step (3) gained roasting 6 ~ 10h under 300 ~ 600 DEG C of nitrogen atmospheres, metal powder carrier is obtained;
(5) equi-volume impregnating is adopted, soluble cobalt is dissolved in deionized water, flood with step (4) gained metal powder carrier at ambient temperature, dip time is 6 ~ 10h, after dipping at 60 ~ 100 DEG C dry 10 ~ 20h, carry out roasting under nitrogen atmosphere after dry, sintering temperature is 200 ~ 400 DEG C, and roasting time is 3 ~ 8h.
2. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, is characterized in that described metal powder carrier is magnesium powder, copper powder, aluminium powder, zinc powder, iron powder, magnesium aluminum-alloy powder or SiCuAl alloyed powder.
3. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, it is characterized in that described metal powder carrier average grain scope 10 ~ 50 μm, specific surface is 70 ~ 650m
2/ g, mesoporous pore size 2 ~ 30nm, macropore diameter 50 ~ 90nm, pore volume is 0.25 ~ 3.00cm
3/ g.
4. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, is characterized in that catalyst specific surface is 50 ~ 600m
2/ g.
5. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, is characterized in that described acid is acetic acid, nitric acid or hydrochloric acid.
6. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, is characterized in that described alkali is potassium hydroxide or NaOH.
7. a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as claimed in claim 1, is characterized in that described cobalt salt is cobalt nitrate or cobalt acetate.
8. the application of a kind of high-termal conductivity Co based Fischer-Tropsch synthesis catalyst as described in any one of claim 1-8, is characterized in that application process is as follows:
(1) catalyst reduces in fixed bed reactors in the hydrogen of 300 ~ 600 DEG C, and reducing gas volume space velocity is 500 ~ 2000h
-1, reduction pressure is 0.1 ~ 1.0Mpa, and the recovery time is 5 ~ 20h;
(2) reaction is carried out in fixed bed reactors, and reaction condition is: H
2the mol ratio of/CO is between 1 ~ 3, and reaction temperature is 190 DEG C ~ 240 DEG C, and pressure is 1.0 ~ 3.0Mpa, and volume space velocity is 500 ~ 2000h
-1.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1778876A (en) * | 2004-11-23 | 2006-05-31 | 北京化工大学 | Metal carrier catalyst for methane catalyzed burning and production thereof |
| CN1781595A (en) * | 2004-12-03 | 2006-06-07 | 中国石油化工股份有限公司 | Foam metal hydrogenating catalyst and its preparing method and use |
| CN101314140A (en) * | 2007-05-31 | 2008-12-03 | 碧氢科技开发股份有限公司 | Porous catalyst structure and its preparation |
| CN101570462A (en) * | 2008-04-30 | 2009-11-04 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis method |
| CN103084218A (en) * | 2013-01-28 | 2013-05-08 | 江苏帕艾尼尔科技有限公司 | Method for loading coating on sponge metal and coating prepared by same |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1778876A (en) * | 2004-11-23 | 2006-05-31 | 北京化工大学 | Metal carrier catalyst for methane catalyzed burning and production thereof |
| CN1781595A (en) * | 2004-12-03 | 2006-06-07 | 中国石油化工股份有限公司 | Foam metal hydrogenating catalyst and its preparing method and use |
| CN101314140A (en) * | 2007-05-31 | 2008-12-03 | 碧氢科技开发股份有限公司 | Porous catalyst structure and its preparation |
| CN101570462A (en) * | 2008-04-30 | 2009-11-04 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis method |
| CN103084218A (en) * | 2013-01-28 | 2013-05-08 | 江苏帕艾尼尔科技有限公司 | Method for loading coating on sponge metal and coating prepared by same |
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