CN106890650A - A kind of catalyst for F- T synthesis and preparation method thereof - Google Patents
A kind of catalyst for F- T synthesis and preparation method thereof Download PDFInfo
- Publication number
- CN106890650A CN106890650A CN201510958601.8A CN201510958601A CN106890650A CN 106890650 A CN106890650 A CN 106890650A CN 201510958601 A CN201510958601 A CN 201510958601A CN 106890650 A CN106890650 A CN 106890650A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- preparation
- synthesis
- carrier
- feature exists
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
-
- 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
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
- C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
Abstract
The present invention relates to a kind of catalyst for F- T synthesis and preparation method thereof, the catalyst for being used for F- T synthesis includes active component and carrier, and the active component is the oxide of Co and Ru or both, and the carrier is silica and/or aluminum oxide, the mass ratio of each component is in catalyst, Co：Ru：Carrier=10-40：0.1-10：50-89.9.The preparation method, comprises the following steps：Catalyst activity component predecessor is prepared, carrier suspension is prepared, catalyst activity component predecessor and carrier suspension are then mixed to prepare catalyst pulp, catalyst pulp obtains finished product through drying, roasting, shaping.The characteristics of catalyst has high metal load capacity and reduction degree high；The catalyst has appropriate pore-size distribution, high activity, high stability, and with low methane selectively and C high5 +Hydrocarbon product selectivity.
Description
Technical field
The present invention relates to a kind of preparation method of catalyst, more particularly to a kind of Co-Ru for F- T synthesis
Catalyst and preparation method thereof.
Background technology
F- T synthesis refer to synthesis gas (H2+ CO) hydrocarbon and other chemicals are produced through catalytic reaction for raw material
Process.Ferrum-based catalyst is cheap and easy to get and the active height of Fischer-Tropsch synthesis, and anti-with WGS high
Should be active, make it particularly suited for low H2/ CO than coal based synthetic gas F- T synthesis.50 years 20th century
In generation, the catalyst that the Sasol companies for being successfully realized F- T synthesis heavy industrialization in South Africa use is exactly
Ferrum-based catalyst.Different, cobalt-base catalyst has good stability, anhydrous gas shift activity because of it,
The features such as thus carbon utilization ratio is high, a most frequently used class of liquid fuel is prepared as natural gas base synthesis gas
Fischer-tropsch synthetic catalyst.It is the reaction for improving the conversion ratio of synthesis gas, hydrocarbon product selectivity and adaptation are used
Device type, the research and development of new fischer-tropsch synthetic catalyst in carrying out always.
Foreign petroleum company successively develops the cobalt-base catalyst with independent intellectual property right.According to key component
Difference, existing Co based Fischer-Tropsch synthesis catalyst can substantially be divided three classes.1. cut during Shell Co. Ltd synthesizes
The Co catalysts used in oily technique (SMDS), consisting of 25Co:0.9Zr、Ti or Cr:100SiO2
(wt), cobalt is supported on silica gel by the method for impregnating or mediate.In 220 DEG C, 2.0MPa and 500h-1
Under the conditions of, the total conversion (CO+H of catalyst2) it is that 75%, C5+ is selectively 82%.2.Exxon (love
It is gram gloomy) company reports Co- noble metals/TiO2Deng with TiO2It is the catalyst of carrier, cobalt is introduced by impregnating.
At 200 DEG C, under the conditions of 2.8MPa and 1000h-1, the CO conversion ratios of catalyst are more than 90%, CH4Choosing
Selecting property is less than 6%, shows excellent reactivity worth.3.Syntroleum (artificial oil) company reports
Co/Al2O3Catalyst system and catalyzing.Above-mentioned catalyst system and catalyzing is respectively provided with activity and choosing high under certain reaction condition
Selecting property.But, because prepared by the above-mentioned most methods using dipping of several catalyst, the pattern of metal is difficult to
Control, and the load capacity of metal is not high enough.In addition with metallic cobalt there is chemical action in carrier, form difficult reduction
Cobalt aluminate (cobaltous silicate, cobalt titanate) class compound, when catalyst runs or in fixed bed in slurry bed system
During middle long time running, the reaction of hydrothermal promotion cobalt and carrier, the restricted lifetime of catalyst causes ton
Oily catalyst cost remains high, and constrains the commercial Application of fischer-tropsch synthesis process.
The content of the invention
It is an object of the invention to provide a kind of catalyst for F- T synthesis and preparation method thereof, the catalyst
With appropriate pore-size distribution, high activity, high stability, and with low methane selectively and C high5 +
Hydrocarbon product selectivity.
To reach above-mentioned purpose, the present invention provides a kind of catalyst for F- T synthesis, including active component
And carrier, the active component for Co and Ru or both oxide, the carrier be silica and/or
Aluminum oxide, the mass ratio of each component is in catalyst, Co：Ru：Carrier=10-40：0.1-10：50-89.9.
Catalyst for F- T synthesis of the present invention, the mass ratio of each component is preferred in the catalyst
For Co：Ru：Carrier=30：0.5：69.5.
The present invention also provides a kind of preparation method of the catalyst for F- T synthesis, and it is above-mentioned catalyst
Preparation method, comprise the following steps：
(1) by catalyst activity component predecessor cobalt nitrate and nitric acid ruthenium be made concentration for 0.05-3 moles/
The mixed solution for rising；It is the urea of 10-400g that quality is added in mixed solution, continuously stirs 0.3-6h,
Hydro-thermal reaction is carried out, reaction temperature is 60-180 DEG C, and the reaction time is 2-20h；Aging 5-6h is stood, from
The heart, washs to sediment；
(2) by carrier predecessor aeroge silica or SB powder aluminum oxide be made into concentration for 50-250 grams/
The carrier suspension for rising；
(3) sediment as obtained by step (1) is added water and is added by step (2) gained after carrying out pulp
Carrier suspension, stir, obtain catalyst pulp；
(4) catalyst pulp as obtained by step (3) is dried 5-30 hours under the conditions of 120 DEG C, so
2-10h is calcined under the conditions of 400-800 DEG C afterwards, cooling, compression molding are crushed, and choose the finished product of 60-80 mesh
As the catalyst of F- T synthesis.
The preparation method of the catalyst for F- T synthesis of the present invention, it is described mixed in step (1)
The concentration for closing solution is preferably 0.1-2 mol/Ls.
The preparation method of the catalyst for F- T synthesis of the present invention, it is described mixed in step (1)
The concentration for closing solution is preferably 0.1-0.5 mol/Ls.
The preparation method of the catalyst for F- T synthesis of the present invention, in step (1), the urine
The quality of element is preferably 30-300g.
The preparation method of the catalyst for F- T synthesis of the present invention, in step (1), the urine
The quality of element is preferably 50-250g.
The preparation method of the catalyst for F- T synthesis of the present invention, it is described anti-in step (1)
Preferably 60-160 DEG C of temperature is answered, the reaction time is preferably 3-15h.
The preparation method of the catalyst for F- T synthesis of the present invention, it is described anti-in step (1)
Preferably 80-140 DEG C of temperature is answered, the reaction time is preferably 5-13h.
The preparation method of the catalyst for F- T synthesis of the present invention, in step (2), the load
The concentration of liquid suspension is preferably 100-200 g/l.
The preparation method of the catalyst for F- T synthesis of the present invention, it is described dry in step (4)
The dry time is preferably 8-20 hours.
The preparation method of the catalyst for F- T synthesis of the present invention, in step (4), the roasting
Burn temperature and be preferably 400-600 DEG C, the roasting time is preferably 3-9h.
The present invention is for the activation condition of catalyst of F- T synthesis：0.1-0.5MPa、1000-5000h-1、
Used hydrogen reducing 13-50 hours under conditions of 300-500 DEG C.
The present invention is used for reaction condition of the catalyst of F- T synthesis in F- T synthesis：180-250℃、
0.5-3.5MPa、300-4000h-1, unstripped gas H2/ CO ratios are 0.5-3.0.
Beneficial effects of the present invention are：
Catalyst for F- T synthesis of the invention is Co and Ru base catalyst, with high metal load
The characteristics of amount and reduction degree high；The catalyst has appropriate pore-size distribution, high activity, high stability, and
With low methane selectively and C high5 +Hydrocarbon product selectivity.
The preparation method of the catalyst for F- T synthesis of the invention, hydro-thermal process is carried out to cobalt precursor,
Make that cobalt-base catalyst has the advantages that regular appearance, metal good crystalline and controllable, particle purity is high.By urging
The scanning electron microscopic picture of agent understands that the catalyst is now laminated structure, the width of piece in microcosmic level upper table
Change with preparation parameter with thickness and change；The precipitating reagent for using is urea, with harmless and low cost, can
Reduce environmental pollution of the baking operation unit to air；Catalyst Preparation Procedures are simplified, while can reduce urging
Agent production cost.
Brief description of the drawings：
Fig. 1 is the scanning electron microscope (SEM) photograph of catalyst prepared by the embodiment of the present invention 1；
Fig. 2 is the scanning electron microscope (SEM) photograph of catalyst prepared by the embodiment of the present invention 2；
Fig. 3 is the scanning electron microscope (SEM) photograph of catalyst prepared by the embodiment of the present invention 3；
Fig. 4 is the scanning electron microscope (SEM) photograph of catalyst prepared by the embodiment of the present invention 4.
Specific embodiment
The present invention is described in further detail by the following examples, but these embodiments are not considered as to this hair
Bright limitation.
Embodiment 1
Weigh Co (NO3)3·6H2O 118g, Ru (NO3)2Solution (in terms of Ru, concentration is 17.25g/L)
20ml, it is 0.9mol/L mixing salt solutions to be configured to total concentration with deionized water, in the salt-mixture for preparing
It is (the NH of 150g that quality is added in solution2)2CO, continuously stirs 2h, pours into the hydro-thermal reaction of 500mL
Kettle is sealed into water-filling thermal response, is put into air dry oven drying, and reaction temperature is 120 DEG C, and the reaction time is
10h.Then aging 5h is stood, suction filtration is washed to sediment repeatedly with deionized water.Add in filter cake
Enter 50mL deionized waters, then ultrasound 10 minutes, mashing.200g silica supports are configured to 25%
Slurries.Above two slurries are mixed, then in 120 DEG C of dryings 10 hours, most after being calcined at 500 DEG C
9h, cooling, compression molding are crushed, and choose 60-80 mesh as fixed bed FischerTropsch synthesis catalyst.The catalysis
Agent part by weight is Co：Ru：Carrier=16：0.2：83.8.
This is used for the catalyst of F- T synthesis, and activation condition is：In 0.3MPa, 1000h-1,350 DEG C of bars
Hydrogen reducing is used under part 30 hours；Then at 180-260 DEG C, 1.5MPa, 1000-3000h-1, unstripped gas
H2Under/CO is than the reaction condition for 2.0, its F- T synthesis performance is evaluated with fixed bed reactors.Reaction knot
Fruit is shown in Table 1.
Embodiment 2：
Weigh Co (NO3)3·6H2O 118g, Ru (NO3)2Solution 100ml, it is configured to always with deionized water
Concentration is 1.5mol/L mixing salt solutions, and it is 100g's that quality is added in the mixing salt solution for preparing
(NH2)2CO, continuously stirs 2h, pours into the hydrothermal reaction kettle sealing of 500mL, is put into air dry oven,
Reaction temperature is 90 DEG C, and the reaction time is 8h.Then aging 5h is stood, suction filtration, with deionized water repeatedly
Sediment is washed.50mL deionized waters are added in filter cake, then ultrasound 10 minutes, mashing.
150g silica supports are configured to 20% slurries.Above two slurries are mixed, slurries are in 120 DEG C of dryings
20 hours, most after 5h is calcined at 400 DEG C, cooling, compression molding were crushed, and choose 60-80 mesh as solid
Fixed bed fischer-tropsch synthetic catalyst.The catalyst weight ratio is Co：Ru：Carrier=20：1.5：78.5.
This is used for the catalyst of F- T synthesis, activation condition and Fischer-Tropsch synthesis condition with embodiment 1, instead
1 should be the results are shown in Table.
Embodiment 3：
Weigh Co (NO3)3·6H2O 128g, Ru (NO3)2Solution 30ml, is configured to total dense with deionized water
It is 0.3mol/L mixing salt solutions to spend, and it is 200g's that quality is added in the mixing salt solution for preparing
(NH2)2CO, continuously stirs 2h, pours into the hydrothermal reaction kettle sealing of 1000mL, is put into air dry oven,
Reaction temperature is 120 DEG C, and the reaction time is 10h.Then aging 5h is stood, suction filtration is anti-with deionized water
It is multiple that sediment is washed.50mL deionized waters are added in filter cake, then ultrasound 10 minutes, mashing.
70g alumina supports are configured to 10% slurries.Above two slurries are mixed, then in 120 DEG C of dryings
10 hours, most after 9h is calcined at 500 DEG C, cooling, compression molding were crushed, and choose 60-80 mesh as solid
Fixed bed fischer-tropsch synthetic catalyst.The catalyst weight ratio is Co：Ru：Carrier=37：0.7：62.3.
This is used for the catalyst of F- T synthesis, and activation condition is：In 0.3MPa, 1000h-1, 350 DEG C of conditions
Lower use hydrogen reducing 30 hours；Then at 180-260 DEG C, 3.5MPa, 1000-3000h-1, unstripped gas H2/CO
Under than the reaction condition for 1.6, the F- T synthesis performance of the catalyst is evaluated for fixed bed reactors.Instead
1 should be the results are shown in Table.
Embodiment 4：
Weigh Co (NO3)3·6H2O 32.5g, Ru (NO3)2Solution 6.5ml, is configured to total dense with deionized water
It is 0.2mol/L mixing salt solutions to spend, and it is 80g's that quality is added in the mixing salt solution for preparing
(NH2)2CO, continuously stirs 2h, pours into the hydrothermal reaction kettle sealing of 1000mL, is put into air dry oven,
Reaction temperature is 120 DEG C, and the reaction time is 10h.Then aging 5h is stood, suction filtration is anti-with deionized water
It is multiple that sediment is washed.50mL deionized waters are added in filter cake, then ultrasound 10 minutes, mashing.
25g alumina supports are configured to 5% slurries.Above two slurries are mixed, then in 120 DEG C of dryings
10 hours, most after 9h is calcined at 400 DEG C, cooling, compression molding were crushed, and choose 60-80 mesh as solid
Fixed bed fischer-tropsch synthetic catalyst.The catalyst weight ratio is Co：Ru：Carrier=30：0.5：69.5.
This is used for the catalyst of F- T synthesis, and activation condition is：In 0.5MPa, 2000h-1, 400 DEG C of conditions
Lower use hydrogen reducing 20 hours；Then at 200-260 DEG C, 3.5MPa, 500-3000h-1, unstripped gas H2/CO
Under than the reaction condition for 2.5, the F- T synthesis performance of the catalyst is evaluated for fixed bed reactors.Instead
1 should be the results are shown in Table.
The reactivity worth and its selectivity of product of each catalyst in the embodiment of table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Reaction temperature (DEG C) | 230 | 250 | 220 | 200 |
| CO conversion ratios (%) | 45.0 | 67.0 | 85.5 | 60.0 |
| Methane selectively (%) | 10.0 | 16.0 | 6.5 | 3.5 |
| 78.0 | 65.1 | 82.3 | 90.8 |
As shown in Table 1, the catalyst for being prepared according to this method, with activity higher and heavy hydrocarbon-selective.
Particularly embodiment 4, the C of catalyst5 +Selectivity shows excellent F- T synthesis performance more than 90%.
Certainly, the present invention can also have other various embodiments, without departing substantially from spirit of the invention and its essence
In the case of, those of ordinary skill in the art can make various corresponding changes and change according to the present invention
Shape, but these corresponding changes and deformation should all belong to protection scope of the present invention.
Claims (12)
1. a kind of catalyst for F- T synthesis, it is characterised in that including active component and carrier, institute
The oxide that active component is Co and Ru or both is stated, the carrier is silica and/or aluminum oxide, is urged
The mass ratio of each component is in agent, Co：Ru：Carrier=10-40：0.1-10：50-89.9.
2. the catalyst for F- T synthesis according to claim 1, it is characterised in that described to urge
The mass ratio of each component is in agent, Co：Ru：Carrier=30：0.5：69.5.
3. the preparation method of a kind of catalyst for F- T synthesis, it is described in claim 1 or 2
The preparation method of catalyst, it is characterised in that comprise the following steps：
(1) by catalyst activity component predecessor cobalt nitrate and nitric acid ruthenium be made concentration for 0.05-3 moles/
The mixed solution for rising；It is the urea of 10-400g that quality is added in mixed solution, continuously stirs 0.3-6h,
Hydro-thermal reaction is carried out, reaction temperature is 60-180 DEG C, and the reaction time is 2-20h；Aging 5-6h is stood, from
The heart, washs to sediment；
(2) by carrier predecessor aeroge silica or SB powder aluminum oxide be made into concentration for 50-250 grams/
The carrier suspension for rising；
(3) sediment as obtained by step (1) is added water and is added by step (2) gained after carrying out pulp
Carrier suspension, stir, obtain catalyst pulp；
(4) catalyst pulp as obtained by step (3) is dried 5-30 hours under the conditions of 120 DEG C, so
2-10h is calcined under the conditions of 400-800 DEG C afterwards, cooling, compression molding are crushed, and choose the finished product of 60-80 mesh
As the catalyst of F- T synthesis.
4. the preparation method of the catalyst for F- T synthesis according to claim 3, its feature exists
In in step (1), the concentration of the mixed solution is 0.1-2 mol/Ls.
5. the preparation method of the catalyst for F- T synthesis according to claim 4, its feature exists
In in step (1), the concentration of the mixed solution is 0.1-0.5 mol/Ls.
6. the preparation method of the catalyst for F- T synthesis according to claim 3, its feature exists
In in step (1), the quality of the urea is 30-300g.
7. the preparation method of the catalyst for F- T synthesis according to claim 6, its feature exists
In in step (1), the quality of the urea is 50-250g.
8. the preparation method of the catalyst for F- T synthesis according to claim 3, its feature exists
In in step (1), the reaction temperature is 60-160 DEG C, and the reaction time is 3-15h.
9. the preparation method of the catalyst for F- T synthesis according to claim 8, its feature exists
In in step (1), the reaction temperature is 80-140 DEG C, and the reaction time is 5-13h.
10. the preparation method of the catalyst for F- T synthesis according to claim 3, its feature exists
In in step (2), the concentration of the carrier suspension is 100-200 g/l.
The preparation method of 11. catalyst for F- T synthesis according to claim 3, its feature exists
In in step (4), the drying time is 8-20 hours.
The preparation method of 12. catalyst for F- T synthesis according to claim 3, its feature exists
In in step (4), the sintering temperature is 400-600 DEG C, and the roasting time is 3-9h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510958601.8A CN106890650A (en) | 2015-12-18 | 2015-12-18 | A kind of catalyst for F- T synthesis and preparation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510958601.8A CN106890650A (en) | 2015-12-18 | 2015-12-18 | A kind of catalyst for F- T synthesis and preparation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106890650A true CN106890650A (en) | 2017-06-27 |
Family
ID=59189789
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510958601.8A Pending CN106890650A (en) | 2015-12-18 | 2015-12-18 | A kind of catalyst for F- T synthesis and preparation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106890650A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109908917A (en) * | 2019-04-11 | 2019-06-21 | 上海兖矿能源科技研发有限公司 | A kind of nanometer iron-based fischer-tropsch synthetic catalyst and its preparation method and application |
| CN113751020A (en) * | 2020-06-03 | 2021-12-07 | 清华大学 | Metal composite compound base noble metal single-atom catalyst material and preparation method thereof |
| CN114749179A (en) * | 2021-01-11 | 2022-07-15 | 中国石油天然气集团公司 | Co/BN catalyst for Fischer-Tropsch synthesis and preparation method and application thereof |
| CN117409877A (en) * | 2023-12-14 | 2024-01-16 | 中国石油大学(华东) | Carbon utilization efficiency evaluation method for thickened oil thermal recovery technology |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101269336A (en) * | 2008-05-19 | 2008-09-24 | 中国科学院山西煤炭化学研究所 | Multilevel hole material load cobalt catalyst, preparation method and application thereof |
| CN102000575A (en) * | 2010-09-20 | 2011-04-06 | 中国科学院山西煤炭化学研究所 | Cobalt-based Fischertropsch synthesis catalyst for slurry-bed reactor, and preparation method and application thereof |
| CN102441403A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Method for preparing cobalt-based Fischer-Tropsch synthetic catalyst |
| CN105013503A (en) * | 2015-06-29 | 2015-11-04 | 中国科学院广州能源研究所 | Preparation method and applications of Fe-based catalyst used for Fischer-Tropsch synthesis |
| CN105107525A (en) * | 2015-02-03 | 2015-12-02 | 天津大学 | Cobalt-based catalyst, and preparation method and application thereof |
-
2015
- 2015-12-18 CN CN201510958601.8A patent/CN106890650A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101269336A (en) * | 2008-05-19 | 2008-09-24 | 中国科学院山西煤炭化学研究所 | Multilevel hole material load cobalt catalyst, preparation method and application thereof |
| CN102000575A (en) * | 2010-09-20 | 2011-04-06 | 中国科学院山西煤炭化学研究所 | Cobalt-based Fischertropsch synthesis catalyst for slurry-bed reactor, and preparation method and application thereof |
| CN102441403A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Method for preparing cobalt-based Fischer-Tropsch synthetic catalyst |
| CN105107525A (en) * | 2015-02-03 | 2015-12-02 | 天津大学 | Cobalt-based catalyst, and preparation method and application thereof |
| CN105013503A (en) * | 2015-06-29 | 2015-11-04 | 中国科学院广州能源研究所 | Preparation method and applications of Fe-based catalyst used for Fischer-Tropsch synthesis |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109908917A (en) * | 2019-04-11 | 2019-06-21 | 上海兖矿能源科技研发有限公司 | A kind of nanometer iron-based fischer-tropsch synthetic catalyst and its preparation method and application |
| CN113751020A (en) * | 2020-06-03 | 2021-12-07 | 清华大学 | Metal composite compound base noble metal single-atom catalyst material and preparation method thereof |
| CN114749179A (en) * | 2021-01-11 | 2022-07-15 | 中国石油天然气集团公司 | Co/BN catalyst for Fischer-Tropsch synthesis and preparation method and application thereof |
| CN117409877A (en) * | 2023-12-14 | 2024-01-16 | 中国石油大学(华东) | Carbon utilization efficiency evaluation method for thickened oil thermal recovery technology |
| CN117409877B (en) * | 2023-12-14 | 2024-03-22 | 中国石油大学(华东) | Carbon utilization efficiency evaluation method for thickened oil thermal recovery technology |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113145155B (en) | Nitrogen-doped carbon-coated nickel catalyst applied to assembly of bioethanol to synthesize high-carbon alcohol and preparation method thereof | |
| CN104324733B (en) | The preparation method of non precious metal high activity photolytic hydrogen production catalyst | |
| CN109718776B (en) | Hydrogenation catalyst Co @ C/biomass and preparation method and application thereof | |
| CN107890870B (en) | Catalyst for preparing methane from carbon dioxide and water, preparation method and application thereof | |
| CN106890650A (en) | A kind of catalyst for F- T synthesis and preparation method thereof | |
| CN107519911B (en) | Nickel-based catalyst prepared by using organic micromolecular additive and application of nickel-based catalyst in methanation reaction | |
| CN105618052A (en) | Fischer-Tropsch synthesizing catalyst prepared by carrying cobalt with porous aluminum oxide, preparation method and application | |
| CN109759064A (en) | A kind of Co@C/ biomass catalyzing agent and its preparation method and application | |
| CN107497439B (en) | Copper-based catalyst for reverse water gas shift reaction and preparation method thereof | |
| CN104815659A (en) | Iron-based catalyst used for Fischer-Tropsch synthesis, preparation method and application | |
| CN105597772B (en) | Cobalt-base catalyst of nucleocapsid and preparation method thereof | |
| CN107233890A (en) | A kind of nickel-base catalyst of attapulgite load of zinc modification and its preparation method and application | |
| CN107335446A (en) | A kind of cobalt-base catalyst and its preparation and application that mixed alcohol is produced for one-step method from syngas | |
| CN105013503B (en) | A kind of preparation method and application of Fe base catalyst for F- T synthesis | |
| CN104707614A (en) | Nickel/gamma-aluminum oxide nano catalyst and synthesis method thereof | |
| WO2021042874A1 (en) | Nickel-based catalyst for carbon dioxide methanation, preparation method therefor and application thereof | |
| CN110368949B (en) | GaFe-based catalyst for preparing low-carbon alcohol by CO hydrogenation, preparation method and application thereof | |
| CN104001538A (en) | Nickel-loaded SBA-15 catalyst modified by cerium dioxide and preparation method and application of nickel-loaded SBA-15 catalyst modified by cerium dioxide | |
| CN114011415A (en) | Preparation method of high-load layered cobalt catalyst for preparing green diesel oil by grease hydrodeoxygenation | |
| CN104815662A (en) | Low-temperature high-activity nano-composite catalyst for methanation of synthesis gas and preparation method thereof | |
| CN103447042A (en) | Preparation method of anti-carbon deposition and anti-sintering monolithic methane dry reforming catalyst | |
| CN102911693B (en) | Fischer-Tropsch synthesis method by employing mixed catalyst | |
| CN106563453A (en) | Composite catalyst for biomass gasification for preparing hydrogen-rich combustion gas, and preparation method thereof | |
| CN108940254B (en) | Preparation method of catalyst for synthesizing methanol by carbon dioxide hydrogenation | |
| CN114160143B (en) | CO (carbon monoxide) 2 Catalyst for preparing methanol by hydrogenation and preparation method and application thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170627 |
|
| RJ01 | Rejection of invention patent application after publication |