CN106540702A - Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof - Google Patents
Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof Download PDFInfo
- Publication number
- CN106540702A CN106540702A CN201611054070.0A CN201611054070A CN106540702A CN 106540702 A CN106540702 A CN 106540702A CN 201611054070 A CN201611054070 A CN 201611054070A CN 106540702 A CN106540702 A CN 106540702A
- Authority
- CN
- China
- Prior art keywords
- liquid hydrocarbon
- base catalyst
- preparation
- catalyst
- metal promoter
- 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
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/80—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
-
- 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
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- 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
- B01J23/8933—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 also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8953—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 also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
-
- 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
-
- 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
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Catalysts (AREA)
Abstract
Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof, is related to fischer-tropsch synthetic catalyst.The Co bases catalyst is defined with M Co/ZnO, and Co is active component, is existed in the form of the oxide, and ZnO is carrier, and M is metal promoter, and metal promoter M is the one kind in Zr, Ti, Al, Ru, is existed in the form of the oxide.Zn saline solution is made by solubility Zn salt soluble in water, it is subsequently adding the soluble metal salt formation mixed solution as metal promoter, by mixed solution constant temperature water bath, add precipitant precipitation, the mixed precipitation serosity of zinc and metal promoter is made, the final ph for adjusting mixed precipitation serosity is 6～10；Solubility Co salt is dissolved in into water Co saline solutions are obtained, in adding mixed precipitation serosity, the mixed sediment serosity containing cobalt is obtained, it is with precipitant regulation pH value to after 6～10, still aging, filter, compression molding after filtration cakes torrefaction, roasting are obtained final product.
Description
Technical field
The present invention relates to a kind of fischer-tropsch synthetic catalyst, is catalyzed more particularly, to the Co bases of co hydrogenation liquid hydrocarbon
Agent and preparation method thereof.
Background technology
F- T synthesis are referred to and for coal, natural gas, biomass technique premenstruum synthesis gas are obtained, and synthesis gas Jing catalyzed conversions are obtained
To hydrocarbon product.Fischer-Tropsch synthesis product is complicated, by the different carbon chain lengths product that gaseous state, liquid and solid-state are presented under room temperature
Composition.Product can obtain the liquid fuel of high added value, i.e. gasoline, diesel oil by the deep processing technique such as be such as polymerized, crack, reforming
And solid product, such as microwax etc..
The core of F- T synthesis technology application is the selection of catalyst.Industrialized fischer-tropsch synthetic catalyst is main at present
It is divided to two classes, i.e. Fe-series catalyst and cobalt series catalyst.Presently disclosed most of fischer-tropsch synthetic catalyst is with Al2O3Or SiO2For
Carrier, patent CN104226315A are disclosed and prepare ZrO with infusion process2Mass content be 1%～10%, CoO be 5%～
25%, remaining is Al2O3Catalyst, fischer-tropsch reaction evaluation result shows that by-product is more, C5 +Selectivity is relatively low.Patent
CN104162441A is disclosed to report and is synthesized Co-Zn-Al fischer-tropsch synthetic catalysts with the sedimentation method, and the catalyst is with Al2O3To carry
Body, ZnO are auxiliary agent, with above-mentioned addition Al2O3The Co/ZnO catalyst of auxiliary agent is compared, and its maximum difference is constituent content
With significant difference.
Di Wanming is in document《Auxiliary agent A l improves the research of Co/ZnO catalyst F-T reactivity worth》It is middle to have investigated different
Preparation method and preparation condition, and auxiliary agent A l2O3Addition for Co/ZnO catalyst fischer-tropsch reaction activity impact.Each
Kind of condition it is preferred under, with catalyst prepared by step-by-step precipitation method, under the conditions of temperature 493K, pressure 2MPa, effectively can carry
The CO conversion ratios of high catalyst.The article pointed out, between the Co/ZnO catalyst carriers prepared using the sedimentation method and active component
Interaction force is weak, is conducive to the reduction of Co, and the granule of carrier Zinc Oxide, than more uniform, aperture is larger, is conducive to what is reacted
Carry out.
(the Applied Catalysis A such as Seon-Ju Park:General, 2012,419-420,148-155) think
In Co/Al2O3Ti is introduced in the preparation process of catalyst, obtained Co/TiO2-Al2O3Catalyst is in temperature 513K, pressure
2000 (hg of 2MPa and gas phase air speedcat.)-1Under the conditions of carry out fischer-tropsch reaction evaluation, work as TiO2Addition be 5wt.% when,
With Co/Al2O3Compare, the CO conversion ratios of catalyst are improved to 57.4% from 34.1%, and C5 +Selectivity from 76.1% increase
To 80.3%.Test result indicate that, TiO2Addition change the acid site density of catalytic surface, while affect catalyst also
The distribution situation of former degree and surface C o granule, so as to significantly improve the reactivity of catalyst.
The content of the invention
It is an object of the invention to provide Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof.
The Co bases catalyst of the co hydrogenation liquid hydrocarbon is defined with M-Co/ZnO, and in formula, Co is active component,
Exist in the form of the oxide, ZnO is carrier, and M is metal promoter, and metal promoter M is the one kind in Zr, Ti, Al, Ru, with oxygen
In the form of compound；By mass percentage, the content of metal promoter M is 5%～25% for the content of 1%～10%, Co,
Balance of ZnO.
The preparation method of the Co base catalyst of the co hydrogenation liquid hydrocarbon, comprises the following steps：
1) will be solubility Zn salt soluble in water, Zn saline solution is made, the soluble metal as metal promoter is subsequently adding
Salt, forms mixed solution, by mixed solution constant temperature water bath, adds precipitant and precipitated, and makes the mixed of zinc and metal promoter
Sediment slurry is closed, the final ph for adjusting mixed precipitation serosity is 6～10；
2) solubility Co salt is dissolved in into water and Co saline solutions is obtained, then Co saline solutions are added into step 1) obtained by mixing it is heavy
In lodgment of stock liquid, the mixed sediment serosity containing cobalt is obtained, then with precipitant regulation pH value to after 6～10, it is still aging；
3) by step 2) still aging gained serosity filtration, after filtration cakes torrefaction, compression molding, roasting obtain final product carbon monoxide
The Co base catalyst of Hydrogenation liquid hydrocarbon.
In step 1) in, the Zn salt may be selected from least one in zinc nitrate, zinc acetate, zinc chloride etc.；The metal
Auxiliary agent may be selected from the one kind in Zr, Ti, Al, Ru etc.；The temperature of the constant temperature water bath can be 50～90 DEG C；The precipitant is optional
One kind from sodium carbonate, ammonium hydrogen carbonate, carbamide, ammonia etc.；The metal promoter M can select respective nitrate, chloride,
At least one in sulfate etc..
In step 2) in, the solubility Co salt may be selected from least one in cobalt nitrate, cobaltous acetate etc.；The precipitant
May be selected from the one kind in sodium carbonate, ammonium hydrogen carbonate, carbamide, ammonia etc.；The still aging time can be 0.5～5h.
In step 3) in, the temperature of the filtration cakes torrefaction can be 60～150 DEG C, and the time of filtration cakes torrefaction can be 5～20h；
The temperature of the roasting can be 400～600 DEG C, and the time of roasting can be 2～10h.
The Co base catalyst of gained co hydrogenation liquid hydrocarbon can be used for reduction treatment and fischer-tropsch reaction liquid hydrocarbon,
Concrete operations flow process is as follows：Reaction evaluating carries out on continuous fixed bed reactor that (quartz reaction bore is about
80mm).Catalyst is located at stove temperature controlling point, and loaded catalyst is 1mL, and particle diameter is 20～40 mesh；Reaction raw materials one are aoxidized
Carbon is 1 ︰ 2 with the mol ratio of hydrogen；Reaction pressure is 2MPa, and feed gas air speed is 1500h-1；Reaction temperature is 200～240
℃.Pretreatment must be carried out before catalyst reaction, under normal pressure low hydrogen atmosphere, 10h is reduced in 400 DEG C.Temperature is adjusted after reduction
It is whole to catalyst desired reaction temperature, question response is carried out after 24h using gas chromatogram to tail gas N2、CO、CO2And C1-C4Product enters
Row on-line analyses, and C5 +Jing hot traps, cold-trap collect off-line analysiss.
Catalyst preparation process of the present invention includes first preparing the mixed serum containing Zn and metal promoter M with coprecipitation, then
Further by Co saline solution addition mixed serum precipitated, most after Jing after still aging, filtration drying and roasting, obtain final product Co bases
Catalyst.Prepared Co bases catalyst carries out Fischer-Tropsch synthesis under appropriate conditions, is keeping higher CO conversion ratios
Very high C can be obtained simultaneously5 +Selectivity and very low methane and carbon dioxide selectivity.
Specific embodiment
The present invention will be further described for example below, but protection scope of the present invention is not by these embodiments
Limit.
Embodiment 1：
Five water zinc nitrates of 16.27g are added in 70mL deionized waters, 0.15g titanium sulfates is added, solution is placed in into water-bath
In the beaker that 90 DEG C of constant temperature, under stirring, in beaker, Deca mass concentration is 20% urea liquid, obtains mixed precipitation serosity,
The pH value of mixed precipitation serosity is adjusted to 7；Weigh 1.81g cabaltous nitrate hexahydrates to be dissolved in 10mL water, cobalt nitrate solution is slow
Be added drop-wise in above-mentioned mixed serum, then the pH value of mixed serum adjusted to 7 with urea liquid, stir 0.5h, by the slurry in beaker
Liquid is put after standing 1h at room temperature, and sucking filtration is dried 10h at 110 DEG C, obtain required catalyst at 500 DEG C after roasting 5h.Will catalysis
Break into pieces after agent compression molding and sieve, the catalyst for taking 20～40 mesh is standby.TiO in catalyst2Weight/mass percentage composition be 1%,
Co3O4Weight/mass percentage composition is 10%, balance of ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Embodiment 2：
The consumption of five nitric hydrate zinc and titanium sulfate in embodiment 1 is changed to into 16.09g and 0.31g respectively, remaining step
With embodiment 1.In prepared catalyst, TiO2Weight/mass percentage composition is 2%, Co3O4Weight/mass percentage composition is 10%, surplus
For ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Embodiment 3：
The consumption of five nitric hydrate zinc and titanium sulfate in embodiment 1 is changed to into 15.53g and 0.75g respectively, remaining step
With embodiment 1.In prepared catalyst, TiO2Weight/mass percentage composition is 5%, Co3O4Weight/mass percentage composition is 10%, surplus
For ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Embodiment 4：
Titanium sulfate in embodiment 1 is substituted for into five nitric hydrate zirconiums of 0.35g, five nitric hydrate zinc 16.09g, remaining step
With embodiment 1.In prepared catalyst, ZrO2Weight/mass percentage composition is 5%, Co3O4Weight/mass percentage composition is 10%, surplus
For ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Embodiment 5：
Titanium sulfate in embodiment 1 is substituted for into 0.37g ANN aluminium nitrate nonahydrates, five nitric hydrate zinc 16.09g, remaining step
With embodiment 1.In prepared catalyst, Al2O3Weight/mass percentage composition is 2%, Co3O4Weight/mass percentage composition is 10%, surplus
For ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Embodiment 6：
Five water zinc nitrates of 16.45g are added in 70mL deionized waters, solution are placed in beaker under 90 DEG C of constant temperature water baths,
Stirring, while to the urea liquid that Deca mass concentration in beaker is 20%, obtaining a mixed precipitation serosity, adjusts mixed precipitation slurry
The pH value of liquid is to 7；Weigh 1.81g cabaltous nitrate hexahydrates and 0.02g ruthenic chlorides are dissolved in 10mL water, by cobalt nitrate and ruthenic chloride
Mixed solution is added drop-wise in above-mentioned serosity, then adjusts pH value to 7 with carbamide, after stirring 0.5h, the serosity in beaker is placed in room
After the lower standing 1h of temperature, sucking filtration is dried 10h at 110 DEG C, obtain required catalyst at 500 DEG C after roasting 5h.By catalyst tabletting into
Break into pieces after type sieve 20～40 mesh catalyst are standby.In prepared catalyst, the weight/mass percentage composition of Ru is 0.1%, Co3O4
Weight/mass percentage composition is 10%, balance of ZnO.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Comparative example 1：
Five water zirconium nitrates of 0.24g are added in 16mL deionized waters, 0.49g beta-schardinger dextrin -s are added, under room temperature, stirs equal
5g 200-300 mesh γ-Al are added after even2O3Powder stirring dipping, heats at 80 DEG C and is evaporated, and 120 DEG C are dried 4h, 400 DEG C
After roasting 5h, the powder infusion is dissolved in into the cobalt nitrate solution in 16mL water in 2.47g cabaltous nitrate hexahydrates, 120 after dipping 24h
DEG C 4h is dried, 400 DEG C of roasting 5h obtain catalyst fines.Compression molding breaks 20～40 mesh catalyst that sieve to obtain into pieces.Prepared
ZrO in catalyst2Weight/mass percentage composition is that 1.18%, CoO weight/mass percentage compositions are 11.15%, balance of γ-Al2O3.Reaction
Raw material carbon monoxide is 1 ︰ 2 with the molar ratio of hydrogen, and reaction pressure is 2MPa, and feed space velocity is 1000h-1；Reaction temperature
At 200～240 DEG C.The fischer-tropsch reaction Evaluation results of catalyst are shown in Table 1.
Comparative example 2：Five water zirconium nitrates and beta-schardinger dextrin-in comparative example 1 are removed, direct impregnation cabaltous nitrate hexahydrate.It is made
In standby catalyst, CoO weight/mass percentage compositions are 11.15%, balance of γ-Al2O3.The fischer-tropsch reaction performance evaluation knot of catalyst
Fruit is shown in Table 1.
Table 1
Table 1 provides the fischer-tropsch reaction Evaluation results of the catalyst of embodiment 1～6 and comparative example 1～2.
Claims (10)
1. the Co base catalyst of co hydrogenation liquid hydrocarbon, it is characterised in that defined with M-Co/ZnO, in formula, Co is activity
Component, is present in the form of the oxide, and ZnO is carrier, and M is metal promoter, and metal promoter M is the one kind in Zr, Ti, Al, Ru,
Exist in the form of the oxide；By mass percentage, the content of metal promoter M for 1%～10%, Co content be 5%～
25%, balance of ZnO.
2. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 1, it is characterised in that bag
Include following steps：
1) will be solubility Zn salt soluble in water, Zn saline solution is made, the soluble metallic salt as metal promoter, shape is subsequently adding
Into mixed solution, by mixed solution constant temperature water bath, add precipitant and precipitated, make the mixed precipitation of zinc and metal promoter
Serosity, the final ph for adjusting mixed precipitation serosity are 6～10；
2) solubility Co salt is dissolved in into water and Co saline solutions is obtained, then Co saline solutions are added into step 1) obtained by mixed precipitation slurry
In liquid, the mixed sediment serosity containing cobalt is obtained, then with precipitant regulation pH value to after 6～10, it is still aging；
3) by step 2) still aging gained serosity filtration, after filtration cakes torrefaction, compression molding, roasting obtain final product co hydrogenation
The Co base catalyst of liquid hydrocarbon processed.
3. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 1) in, at least one of the Zn salt in zinc nitrate, zinc acetate, zinc chloride.
4. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 1) in, the one kind of the metal promoter in Zr, Ti, Al, Ru.
5. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 1) in, the temperature of the constant temperature water bath is 50～90 DEG C.
6. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 1) in, the one kind of the precipitant in sodium carbonate, ammonium hydrogen carbonate, carbamide, ammonia.
7. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 1) in, the metal promoter is from least one in respective nitrate, chloride, sulfate.
8. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 2) in, at least one of the solubility Co salt in cobalt nitrate, cobaltous acetate；The precipitant may be selected from sodium carbonate,
One kind in ammonium hydrogen carbonate, carbamide, ammonia；The still aging time can be 0.5～5h.
9. the preparation method of the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 2, it is characterised in that
Step 3) in, the temperature of the filtration cakes torrefaction is 60～150 DEG C, and the time of filtration cakes torrefaction is 5～20h；The temperature of the roasting
It can be 400～600 DEG C, the time of roasting can be 2～10h.
10. the Co base catalyst of co hydrogenation liquid hydrocarbon as claimed in claim 1 is in reduction treatment and fischer-tropsch reaction system
Apply in liquid hydrocarbon.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611054070.0A CN106540702A (en) | 2016-11-25 | 2016-11-25 | Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611054070.0A CN106540702A (en) | 2016-11-25 | 2016-11-25 | Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106540702A true CN106540702A (en) | 2017-03-29 |
Family
ID=58395130
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611054070.0A Pending CN106540702A (en) | 2016-11-25 | 2016-11-25 | Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106540702A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116173959A (en) * | 2022-12-12 | 2023-05-30 | 陕西科技大学 | Reverse ZrO 2 -Co catalyst and catalytic Co thereof 2 Hydrogenation synthesis C 5+ Use of alkanes |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101327430A (en) * | 2008-07-30 | 2008-12-24 | 中国科学院山西煤炭化学研究所 | Cobalt-based catalyst for producing heavy hydrocarbon from synthesis gas and preparation and use thereof |
| CN102908957A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Method for Fischer-Tropsch synthesis |
| WO2014173229A1 (en) * | 2013-04-25 | 2014-10-30 | 武汉凯迪工程技术研究总院有限公司 | Fischer-tropsch synthesis catalyst for syngas to low carbon olefins, modified molecular sieve carrier and preparation method thereof |
| CN104226315A (en) * | 2014-09-30 | 2014-12-24 | 厦门大学 | Co-based catalyst used for preparing hydrocarbon mixture through CO hydrogenation and preparation method thereof |
-
2016
- 2016-11-25 CN CN201611054070.0A patent/CN106540702A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101327430A (en) * | 2008-07-30 | 2008-12-24 | 中国科学院山西煤炭化学研究所 | Cobalt-based catalyst for producing heavy hydrocarbon from synthesis gas and preparation and use thereof |
| CN102908957A (en) * | 2011-08-01 | 2013-02-06 | 中国石油化工股份有限公司 | Method for Fischer-Tropsch synthesis |
| WO2014173229A1 (en) * | 2013-04-25 | 2014-10-30 | 武汉凯迪工程技术研究总院有限公司 | Fischer-tropsch synthesis catalyst for syngas to low carbon olefins, modified molecular sieve carrier and preparation method thereof |
| CN104226315A (en) * | 2014-09-30 | 2014-12-24 | 厦门大学 | Co-based catalyst used for preparing hydrocarbon mixture through CO hydrogenation and preparation method thereof |
Non-Patent Citations (1)
| Title |
|---|
| XIAOQIN WANG,ET AL: ""Influences of Al2O3 on the structure and reactive performance of Co/ZnO catalyst", 《CATALYSIS COMMUNICATIONS》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116173959A (en) * | 2022-12-12 | 2023-05-30 | 陕西科技大学 | Reverse ZrO 2 -Co catalyst and catalytic Co thereof 2 Hydrogenation synthesis C 5+ Use of alkanes |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101310856B (en) | Catalyst for directly synthesizing high carbon primary alcohol using CO hydrogenation and preparation method thereof | |
| CN104096564B (en) | A kind of Fischer-Tropsch synthetic iron-based catalyst and its preparation method and application | |
| CN102489340B (en) | Method for preparing catalyst used for one-carbon chemical reactions through coprecipitation | |
| CN110327933A (en) | Hydrogenation of carbon dioxide prepares catalyst of methanol and its preparation method and application | |
| CN110102294B (en) | Composite oxide loaded Pd-based catalyst, and preparation method and application thereof | |
| CN104624196B (en) | A kind of high-specific surface area fischer-tropsch synthetic catalyst and preparation method and application | |
| CN115254100A (en) | For CO 2 Preparation and application of metal oxide doped type monatomic catalyst for preparing ethanol by hydrogenation | |
| CN112808291B (en) | Preparation method of Co-Zn/C-N catalyst and application of Co-Zn/C-N catalyst in CO 2 Application of hydrogenation methanol synthesis reaction | |
| KR102035714B1 (en) | Nickel catalysts for reforming hydrocarbons | |
| CN109012665A (en) | A kind of double coating three-way catalysts and preparation method thereof | |
| CN104645981A (en) | Pyrolysis gasoline hydrogenation catalyst and preparation method thereof | |
| CN106607053B (en) | Synthesis gas directly prepares Fe-Mn series catalysts of low-carbon alkene and preparation method thereof | |
| WO2019183842A1 (en) | Composite catalyst, preparation method therefor and method for preparing ethylene | |
| CN104014345A (en) | CuO-CeO2 catalyst for water gas conversion reaction and preparation method thereof | |
| KR20170005475A (en) | Catalyst suitable for production of aviation kerosene from biomass fischer-tropsch synthesis oil and preparation method therefor | |
| CN105435799A (en) | Catalyst for ethanol preparation by ethyl acetate hydrogenation and preparation method for catalyst | |
| CN104588033B (en) | Slurry bed Fischer-Tropsch synthesis catalyst, and preparation method and application thereof | |
| CN106540702A (en) | Co base catalyst of co hydrogenation liquid hydrocarbon and preparation method thereof | |
| CN105214688A (en) | A kind of Co based Fischer-Tropsch synthesis catalyst and preparation method thereof | |
| JP2010530305A (en) | Process for the preparation of cobalt-zinc oxide Fischer-Tropsch catalyst | |
| CN111068687A (en) | Catalyst for preparing low-carbon olefin by synthesis gas one-step method and application thereof | |
| CN1044569C (en) | Titania support and its production and application | |
| CN106423202A (en) | Preparation method of rhodium-ruthenium composite catalyst for preparing ethyl alcohol through acetic acid hydrogenation | |
| CN106582638A (en) | Preparation method of (Au,Rh)-Cex/Al2O3 applied to NO+CO reaction | |
| CN101966461B (en) | Superfine cobalt-based catalyst for slurry bed reactor and preparation and application thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170329 |