CN107020154A - A kind of preprocess method of the cobalt-base catalyst activity of raising CO Hydrogenation alkene - Google Patents
A kind of preprocess method of the cobalt-base catalyst activity of raising CO Hydrogenation alkene Download PDFInfo
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- 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
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Abstract
The invention discloses a kind of preprocess method of the cobalt-base catalyst of raising CO Hydrogenation alkene activity, the operation that multiple reduction and carbonization is reduced is used to the cobalt-base catalyst after roasting, cobalt-base catalyst can be promoted to the selectivity and stability of total olefin.Reducing condition is in this method：Atmosphere is the gaseous mixture of hydrogen or hydrogen and other gases, 200~750 DEG C of temperature, 0.1~4.0MPa of pressure, 0.5~48h of time, 1000~30000mL/g/h of air speed；Carbonization Conditions：Atmosphere is carbon monoxide or carbon dioxide or lower carbon number hydrocarbons or their gaseous mixtures with other gases；200~750 DEG C of temperature, 0.1~3.0MPa of pressure, 0.5~48h of time, 1000~30000mL/g/h of air speed.By treated catalyst, total olefin (C2 C12) selectivity can be significantly improved, while the stability of catalyst is improved.
Description
Technical field
The invention belongs to synthesis gas transformation technology field, more particularly to a kind of cobalt-based catalyst of raising CO Hydrogenation alkene
The preprocess method of agent activity.
Background technology
C2-C12 alkene is important industrial chemicals, and it is mainly derived from the cracking of naphtha.With subtracting for crude resources
Few and environmental problem becomes increasingly conspicuous, while the exploitation of shale gas scale so that obtain alkene from petroleum path and be challenged,
Also become unsustainable.Therefore, Non oil-based route preparing low-carbon olefins are increasingly taken seriously.The direct producing light olefins of synthesis gas
As a substitute technology route of the production low-carbon alkene such as ethene and propylene, for being provided using China compared with the coal of horn of plenty
The dependence of source, alleviation to petroleum resources, it is significant.The technique need not be as indirect method technique from synthesis gas through methanol
Or dimethyl ether, further prepare alkene, simplification of flowsheet, running cost is low, greatly reduce investment.
Synthesis gas alkene directly processed refers to synthesis gas (CO and H2) under catalyst action, difference is made by F- T synthesis
The process of the alkene of carbon number, the process byproduct water and CO2.Because Fischer-Tropsch synthetic distribution is by Anderson-Schulz-
The limitation of Flory rules (chain increases the molar distribution according to exponential decrease), and the strongly exothermic property of reaction is easily caused methane and low-carbon
The generation of alkane, and promote the alkene of generation to occur secondary response, it is desirable to it is more difficult to obtain alkene with high selectivity, crucial to exist
Exploitation and catalyst handling techniques in high performance catalyst.
Traditional synthesis gas directly prepare alkene catalyst mainly based on iron-based (CN105964263A,
CN105195169A, CN104888838A), although ferrum-based catalyst has preferable catalytic activity and olefine selective, but these
Catalyst is usually predominantly that higher olefins are less based on low-carbon alkene (C2-C4 alkene).With some Fine Chemicals pair
Higher olefins demand constantly increases, it is necessary to develop new fischer-tropsch synthetic catalyst or new processing method.In addition, Fe bases are urged
Inevitably contain iron oxide composition in agent, to promote the progress of water gas shift reaction, cause CO2Selectivity compared with
Height, reduces CO utilization rate.Cobalt-base catalyst is generally insensitive to water gas shift reaction in fischer-tropsch reaction, but its chain increases
Long ability and hydrogenation capability are better than ferrum-based catalyst, and this is caused in fischer-tropsch reaction product based on High-carbon alkane, rarer alkene
Produce.Make the selectivity that alkene is improved on cobalt-base catalyst, it usually needs addition such as Mn auxiliary agents (CN105107523A).
Therefore need to set up a kind of cobalt-base catalyst preprocess method simple and easy to apply, may be such that cobalt-base catalyst has preferable activity
And selectivity of light olefin, while water gas shift reaction can be reduced, that is, reduce CO2Selectivity.
The content of the invention
The invention provides a kind of preprocess method of the cobalt-base catalyst of raising CO Hydrogenation alkene activity, this method letter
Single easy, the catalyst after processing is that can increase the selectivity of total olefin, is gathered while active specy cobalt particle can be prevented effectively from
Collection, maintains its high dispersion state, can also improve the life-span of catalyst.
Active component decentralization and the activity in fischer-tropsch reaction, cobalt-based of the invention in cobalt-base catalyst are improved to realize
Catalyst processing method is the circulate operation that multiple reduction-carbonization-reduction is used to the cobalt-base catalyst after roasting.Circulate operation
Number of times is 1~10 time, preferably 1~3 time.
The restoring operation condition being related in the inventive method is：Reducing atmosphere is the mixing of hydrogen or hydrogen and other gases
Gas；Temperature is 200~750 DEG C, preferably 300~550 DEG C；Pressure is 0.1~4.0MPa, preferably 0.1~2.0MPa；Processing time
0.5~48h, preferably 3~12h；Handle 1000~30000mL/g/h of air speed, preferably 3000~15000mL/g/h.The carbon being related to
Changing operating condition is：Carburizing atmosphere is carbon monoxide or carbon dioxide or lower carbon number hydrocarbons or their gaseous mixtures with other gases；Temperature
Spend for 200~750 DEG C, preferably 300~500 DEG C；Pressure is 0.1~3.0MPa, preferably 0.1~1.0MPa；Processing time 0.5~
48h, preferably 3~12h；Handle 1000~30000mL/g/h of air speed, preferably 3000~15000mL/g/h.
Other gases described in the inventive method are one or more in nitrogen, argon gas, hydrogen and helium, other
The percentage by volume of gas is 1%~99%, preferably 80%~99%.
In cobalt-base catalyst described in the inventive method, the percetage by weight content of cobalt is 8%~60%, preferably 10%
~35%.The precursor of cobalt is the soluble-salt of cobalt, preferably cobalt nitrate, cobalt acetate and cobalt chloride.Auxiliary agent percetage by weight content
For 0.1-15%, preferably 0.3-5%, auxiliary element is K, Na, Mn, S, Cu, more than one or both of Fe.Calcination atmosphere leads to
It is often air or nitrogen, sintering temperature is 200 DEG C~600 DEG C, roasting time 1h~24h.Cobalt-based after the inventive method processing
Catalyst can be used for F- T synthesis catalytic reaction, and reaction condition is：Reaction temperature is 150 DEG C~400 DEG C, synthesizes atmospheric pressure
0.1MPa~4MPa, H2Mol ratio with CO is 0.1~5, and air speed is 1000mL/g/h~50000mL/g/h.
Advantages of the present invention is as follows：
(1) multiple reduction and carbonization restoring operation is used to cobalt-based loaded catalyst, is conducive to cobalt particle to disperse and formed
High activity cobalt granule (Fig. 1), beneficial to the selectivity for improving total olefin, reduces the selectivity of total alkane.
(2) simultaneously, the invention processing method can also avoid cobalt particle agglomeration during the course of the reaction, it is to avoid catalyst
Rapid deactivation, so as to extend the life-span of catalyst.
Brief description of the drawings
Fig. 1 is the schematic diagram of cobalt-base catalyst method processed by the invention before and after the processing after roasting.
Embodiment
The technology of the present invention details is described in detail by following embodiments.It should be noted that for embodiment, its
Effect simply further illustrates the technical characteristic of the present invention, rather than limits the present invention.Meanwhile, embodiment has been merely given as realizing
The partial condition of this purpose, is not meant to that this purpose can just be reached by must being fulfilled for these conditions.
Embodiment 1
Take with Co (NO3)2The 25wt%Co/SiO prepared for cobalt precursor and using equi-volume process2Catalyst is (in air
500 DEG C of roasting 5h, 40~60 mesh) 1g, after uniformly being mixed with 2g quartz sands, it is filled into fixed bed reactor, carries out 450
In DEG C hydrogen (30mL/min, 0.1MPa) reduction 8h and carbon in 300 DEG C of carbon monoxide (30mL/min, 0.1MPa) is cooled to afterwards
Changing 5h, then reduction treatment 5h reduction and carbonization is reduced 1 time in 300 DEG C of hydrogen again, and end temperature is down to 240 DEG C and introduces hydrogen
Gas and the synthesis gas that carbon monoxide mole ratios are 2, regulation pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out F- T synthesis
Reaction, reaction result is shown in Table 1.
Embodiment 2
Take with Co (NO3)2For cobalt precursor and with Mn (NO3)2For Mn auxiliary agents presoma and using the side of isometric co-impregnation
1.2wt%Mn-25wt%Co/SiO prepared by method2Catalyst (500 DEG C of roasting 5h, 40~60 mesh in air) 1g, with 2g quartz
Sand uniformly after mixing, is filled into fixed bed reactor, carries out reduction 8h in 450 DEG C of hydrogen (30mL/min, 0.1MPa)
And carbonization 5h and then the reduction treatment in 300 DEG C of hydrogen again in 300 DEG C of carbon monoxide (30mL/min, 0.1MPa) are cooled to afterwards
5h reduction and carbonization reduction circulation 2 times, it is 2 synthesis that end temperature, which is down to 240 DEG C and introduces hydrogen and carbon monoxide mole ratios,
Gas, regulation pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, and reaction result is shown in Table 1.
Embodiment 3
Take with Co (NO3)3For cobalt precursor and with Mn (Ac)2Prepared for Mn auxiliary agents presoma and using equi-volume process
3wt%Mn-20wt%Co/Al2O3Catalyst (500 DEG C of roasting 5h, 40~60 mesh in air) 1g, is uniformly mixed with 2g quartz sands
Afterwards, it is filled into fixed bed reactor, carries out reducing 8h in 450 DEG C of hydrogen (30mL/min, 0.1MPa) and cool afterwards
Into 300 DEG C of ethene (30mL/min, 0.1MPa) carbonization 5h then again in 300 DEG C of hydrogen reduction treatment 5h reduction and carbonization is also
Former 1 time, end temperature is down to 240 DEG C and introduces hydrogen and the synthesis gas that carbon monoxide mole ratios are 2, and regulation pressure is arrived
1.0MPa, air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, and reaction result is shown in Table 1.
Embodiment 4
Take with Co (Ac)2The 20wt%Co/Al prepared for cobalt precursor and using equi-volume process2O3Catalyst is (in air
500 DEG C of roasting 5h, 40~60 mesh) 1g, after uniformly being mixed with 2g quartz sands, it is filled into fixed bed reactor, carries out 450
In DEG C hydrogen (30mL/min, 0.1MPa) reduction 8h and the gaseous mixture (1 of 300 DEG C of carbon monoxide and hydrogen is cooled to afterwards:1,
30mL/min, 0.1MPa) middle carbonization 5h, then reduction treatment 5h reduction and carbonization reduction is circulated 2 times in 300 DEG C of hydrogen again,
End temperature is down to 240 DEG C and introduces hydrogen and the synthesis gas that carbon monoxide mole ratios are 2, regulation pressure to 1.0MPa, air speed
For 4500mL/g/h, Fischer-Tropsch synthesis is carried out, reaction result is shown in Table 1.
Embodiment 5
Take with CoCl2The 20wt%Co/SiO prepared for cobalt precursor and using equi-volume process2Catalyst is (500 DEG C in air
It is calcined 5h, 40~60 mesh) 1g, after uniformly being mixed with 2g quartz sands, it is filled into fixed bed reactor, carries out 450 DEG C of hydrogen
8h is reduced in gas (30mL/min, 0.1MPa) and carbonization 5h in 300 DEG C of carbon monoxide (30mL/min, 0.1MPa) is cooled to afterwards
Then again in 300 DEG C of hydrogen reduction treatment 5h reduction and carbonization 1 time, end temperature is down to 240 DEG C and introduces hydrogen and an oxygen
Change the synthesis gas that carbon mol ratio is 0.5, regulation pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, instead
1 should be the results are shown in Table.
Embodiment 6
Take with CoCl2For cobalt precursor and with Mn (Ac)2Prepared for Mn auxiliary agents presoma and using equi-volume process
1.0wt%Mn-20wt%Co/SiO2Catalyst (500 DEG C of roasting 5h, 40~60 mesh in air) 1g, is uniformly mixed with 2g quartz sands
After conjunction, it is filled into fixed bed reactor, carries out reducing 8h in 450 DEG C of hydrogen (30mL/min, 0.1MPa) and drop afterwards
In temperature to 300 DEG C of carbon monoxide (30mL/min, 0.1MPa) carbonization 5h then again in 300 DEG C of hydrogen reduction treatment 5h reduction
Carbonizing reduction is circulated 2 times, and end temperature is down to 240 DEG C and introduces hydrogen and the synthesis gas that carbon monoxide mole ratios are 0.5, regulation
Pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, and reaction result is shown in Table 1.
Comparative example 1
Take with Co (NO3)2The 20wt%Co/SiO prepared for cobalt precursor and using equi-volume process2Catalyst is (in air
500 DEG C of roasting 5h, 40~60 mesh) 1g, after uniformly being mixed with 2g quartz sands, it is filled into fixed bed reactor, only carries out
Reduction 5h in 500 DEG C of hydrogen (30mL/min, 0.1MPa), subsequent temperature is down to 230 DEG C and introduces hydrogen and carbon monoxide mole
Than the synthesis gas for 2, regulation pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, and reaction result is shown in Table
2。
Comparative example 2
Take with Co (NO3)2For cobalt precursor and with Mn (NO3)2For Mn auxiliary agents presoma and using the side of isometric co-impregnation
3wt%Mn-20wt%Co/Al prepared by method2O3Catalyst (500 DEG C of roasting 5h, 40~60 mesh in air) 1g, with 2g quartz sands
After uniform mixing, it is filled into fixed bed reactor, only carries out reduction 5h in 500 DEG C of hydrogen (30mL/min, 0.1MPa),
Subsequent temperature is down to 230 DEG C and introduces hydrogen and the synthesis gas that carbon monoxide mole ratios are 2, regulation pressure to 1.0MPa, air speed
For 4500mL/g/h, Fischer-Tropsch synthesis is carried out, reaction result is shown in Table 2.
Comparative example 3
Take with Co (NO3)2The 20wt%Co/Al of method preparation for cobalt precursor and using incipient impregnation2O3Catalyst
(500 DEG C of roasting 5h, 40~60 mesh in air) 1g, after uniformly being mixed with 2g quartz sands, is filled into fixed bed reactor,
Carry out reducing 5h in 500 DEG C of hydrogen (30mL/min, 0.1MPa) and be cooled to the gaseous mixture of 300 DEG C of carbon monoxide and hydrogen afterwards
(1:1,30mL/min, 0.1MPa) in carry out carbonization 5h, then temperature be down to 230 DEG C and be introduced directly into hydrogen and one without reduction
Carbonoxide mol ratio is 2 synthesis gas, and regulation pressure is to 1.0MPa, and air speed is 4500mL/g/h, carries out Fischer-Tropsch synthesis, instead
2 should be the results are shown in Table.
Fischer-Tropsch catalytic reaction result in the embodiment of table 1
Note：A) reaction condition is 240 DEG C, 1.0MPa, H2/ CO=2, air speed 4500mL/g/h；b)H2/ CO=0.5, air speed
8000mL/g/h.Each embodiment catalyst keeps activity stabilized in 100h, and data are the average value in 2~100h in table.
Fischer-Tropsch catalytic reaction result in the comparative example of table 2
Note：Reaction condition is 230 DEG C, 1.0MPa, H2/ CO=2, air speed 4500mL/g/h；Each comparative example catalyst is preceding
Activity is kept to stablize relatively in 20h, then slow inactivation, data are the average value in 2~20h in table.
Contrast Tables 1 and 2 result can be seen that the pre- place that reduction and carbonization reduction is employed for conventional cobalt-base catalyst
After reason operation, the selectivity of total olefin can be significantly improved, while the reaction stability of catalyst is also improved obviously.
Claims (6)
1. the preprocess method of the cobalt-base catalyst activity of a kind of raising CO Hydrogenation alkene, it is characterised in that after roasting
Cobalt-base catalyst uses the circulate operation that multiple reduction and carbonization is reduced, and the circulate operation number of times of reduction and carbonization reduction is 1~10 time,
It is preferred that 1~3 time.
2. according to the method described in claim 1, it is characterised in that reducing condition is：Reducing atmosphere is hydrogen or hydrogen and its
The gaseous mixture of its gas；Temperature is 200~750 DEG C, preferably 300~550 DEG C；Pressure be 0.1~4.0MPa, preferably 0.1~
2.0MPa；0.5~48h of processing time, preferably 3~12h；Handle 1000~30000mL/g/h of air speed, preferably 3000~
15000mL/g/h。
3. according to the method described in claim 1, it is characterised in that Carbonization Conditions are：Carburizing atmosphere is carbon monoxide or dioxy
Change carbon or lower carbon number hydrocarbons or their gaseous mixtures with other gases；Temperature is 200~750 DEG C, preferably 300~500 DEG C；Pressure is
0.1~3.0MPa, preferably 0.1~1.0MPa；0.5~48h of processing time, preferably 3~12h；Processing air speed 1000~
30000mL/g/h, preferably 3000~15000mL/g/h.
4. according to method according to any one of claims 1 to 3, it is characterised in that other gases be nitrogen, argon gas, hydrogen,
With one or more in helium, the percentage by volume of other gases is 1%~99%, preferably 80%~99%.
5. according to the method described in claim 1, it is characterised in that the percetage by weight content of cobalt in described cobalt-base catalyst
For 8%~60%, preferably 10%~35%；The precursor of cobalt is the soluble-salt of cobalt, preferably cobalt nitrate, cobalt acetate and chlorination
Cobalt.Auxiliary agent percetage by weight content is 0.1-15%, preferably 0.3-5%, and auxiliary element is K, Na, Mn, S, Cu, one kind in Fe
Or it is two or more.
6. according to the method described in claim 1, it is characterised in that described cobalt-base catalyst can be used for F- T synthesis catalysis anti-
Should, reaction condition is：Reaction temperature is 150 DEG C~400 DEG C, synthesis atmospheric pressure 0.1MPa~4MPa, H2Mol ratio with CO is
0.1~5, air speed is 1000mL/g/h~50000mL/g/h.
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| CN114369003A (en) * | 2020-10-14 | 2022-04-19 | 中国石油天然气股份有限公司 | Pretreatment method of catalyst for synthesizing alpha-olefin |
| CN112808295A (en) * | 2021-01-15 | 2021-05-18 | 昆明理工大学 | Preparation method and application of single-site Co (II) catalyst |
| CN112808295B (en) * | 2021-01-15 | 2022-03-22 | 昆明理工大学 | Preparation method and application of single-site Co (II) catalyst |
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Application publication date: 20170808 |