CN103468298B - Method for converting biomass synthesis gas into liquid fuel by Fischer-Tropsch reaction - Google Patents
Method for converting biomass synthesis gas into liquid fuel by Fischer-Tropsch reaction Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention relates to a method for converting biomass synthesis gas into liquid fuel by a Fischer-Tropsch reaction. The method comprises the steps of enabling a biomass material to be gasified into the biomass synthesis gas in water vapor and oxygen medium, and converting the biomass synthesis gas into C5-C20 liquid alkane fuel by the Fischer-Tropsch reaction. The Fischer-Tropsch reaction of the biomass synthesis gas adopts a gas-solid reaction, and takes a fixed bed as a reactor and a solid load type catalyst with a certain form as a catalyst of the reaction. The main catalyst metal of the catalyst is Co, a carrier of the catalyst is a single oxide or a composite oxide, and the promoter metal of the catalyst comprises one or two selected from Re, Ru, Cu, Mg, Zr or Pt. The conversion temperature of the biomass synthesis gas is 180-230 DEG C, and the reactant gas pressure is lower than 1.0MPa. The single pass conversion rate of biomass synthesis gas is nearly 90%. The invention provides an effective way for synthesizing the liquid fuel by a renewable raw material.
Description
Technical field
The invention belongs to biomass energy efficient utilization field, it is related to react living beings by fischer-tropsch
The method that synthesis gas is converted into liquid fuel.
Background technology
The energy is divided into non-renewable energy resources and regenerative resource.Non-renewable energy resources include coal, oil and natural gas.Can be again
The raw energy includes water energy, wind energy, solar energy, tide energy, sea wave energy, geothermal energy, ocean heat, Hydrogen Energy, nuclear energy, bioenergy.?
2007, global coal output was 6.5 × 109T, and the amount of whole world coal is 9.09 × 1011If t is that is to say, that press
According to this speed, coal only enough 140 years.The coal power station substantial amounts of pollution of discharge every year: 1.1 × 107T carbon dioxide, 3 × 104T nitrogen
Oxide, 1.6 × 104T sulfur dioxide, 1 × 103T dust and other a small amount of picture calcium, potassium, the chemical substance such as titanium and arsenic.With
The speed of production of present oil, global oil at most can only be with 50 years.1996, the reserves of global natural gas were
1.412×1015m3, only with more than 60 years.So, it is necessary and urgent for greatly developing regenerative resource.
At present, the discharge of China's greenhouse gases exceedes 13% that world's total emission volumn requires, with economic rapid growth,
The discharge of greenhouse gases presents a rapidly rising trend.Renewable Energy Development is to improve Chinese energy safety, Optimization of Energy Structure,
Through obtaining the great attention of country.2 months 28 Shi Jie Standing Committee of the National People's Congress the 14th meeting in 2005 passes through that " the Chinese people are altogether
With state's renewable resource method " Article 16 explicitly point out " country encourage cleaning, efficiently develop biomass fuel, encourage
Development energy crop ".
Living beings are the organic substances that luminous energy is stored with chemical energy form.Its main composition includes: half fiber
Element, cellulose and lignin.The utilization ways of biomass energy have two kinds: thermochemical study and biochemical process conversion.Heat chemistry
Conversion has three kinds of modes: in excess air, living beings are directly burnt generation heat, gasifies as synthesis gas under the conditions of gasifying medium,
Fast pyrogenation is biomass liquid fuel under anaerobic；Bio-ethanol, biogas, hydrogen can be obtained by biochemical conversion process
With other chemicals.As a kind of reproducible energy form, it has 4 points of advantages to living beings, first, it is can to hold in future
The renewable resource of continuous exploitation；Second, replacement fossil energy, discharge and oxynitrides and the sulfur-bearing dirt of greenhouse gases can be reduced
The discharge of dye thing；Third, the economy of rural areas can be developed, increase farmers' income；Fourth, exploitation marginal land and uncomfortable grain
The farmland planting energy crop of food crop.
In Biomass Energy Utilization, gasification of biomass is the thermochemical study mistake comparatively having more practical application meaning
Journey.Gasification of biomass produces synthesis gas, and synthesis gas can be converted into alkane liquid fuel by fischer-tropsch reaction.
Fischer-tropsch reaction is the technology of a class comparative maturity, is applied to for coal to be converted into liquid by synthesis gas former in early days
Material (coal to liquid, ctl).First by this process industrialization, its application scale also constantly expands the sasol in South Africa.
The coal that domestic Shenhua Group also establishes based on fischer-tropsch reaction becomes the demonstration plant of oil.In the recent period,
The rise of fischer-tropsch reaction is mainly based upon liquid fuel (the gas to that natural gas is converted into cleaning
Liquid, gtl) needs, shell is successfully established the fischer- of extensive raw material based on natural gas in Qatar
The industrial plants of tropsch synthetic liquid fuel.Compare by coal and natural gas preparation synthesis gas, biomass synthesis gas pure
Degree, c/h ratio is all poorly suited for traditional fischer-tropsch course of reaction.In order to realize leading to biomass efficient
Cross fischer-tropsch reaction and be converted into liquid alkane fuel (biomass to liquid, btl) it is necessary to exploitation can be special
For biomass synthesis gas fischer-tropsch catalyst.
The present invention is a kind of fischer-tropsch(Fischer-Tropsch being suitable to biomass synthesis gas) catalysts system.Raw
Material synthesis gas is converted into the liquid alkane fuel of c5-c20 by this process.Due to the present invention be directed to biomass synthesis gas
Design, so this method for transformation of the present invention has very big advantage it is contemplated that can apply to renewable money to a certain extent
The liquid fuel synthesis in source.
Content of the invention
It is an object of the invention to provide a kind of be converted into liquid by fischer-tropsch reaction by biomass synthesis gas
The method of fuel.
Biomass synthesis gas are converted into liquid fuel by a kind of the reaction by fischer-tropsch that the present invention provides
Method: biomass synthesis gas are converted into alkane liquid fuel, described alkane liquid in the fixed bed reactors be filled with catalyst
Fluid fuel is collected by direct water-cooling；
Described catalyst is formed by the primary catalyst metal of supported on carriers and co-catalysis metal, wherein main catalytic
The load capacity of agent metal is 10～20wt% of vehicle weight；Described promoter metal and described primary catalyst metal
The mass values of material are 0.01～2.0；
Described primary catalyst metal is cobalt, and described promoter metal is selected from re, ru, cu, mg, zr and pt one
Plant or any two kinds.
Preferably, described catalyst is prepared by following methods:
By the promoter metal of the precursor of the primary catalyst metal of 5.0～9.9 weight portions and 0.01～5.0 weight portion
Precursor is dissolved in 150 parts by volume deionized waters, is heated to seething with excitement；The carrier of 8～12 weight portions adds thermosol under fast stirring
Xie Zhong, continues heating stirring to carrier dried, obtains catalyst precarsor, wherein, described weight portion: and described parts by volume=gram: in the least
Rise, then again gained catalyst precarsor is heated to 300 DEG C in atmosphere and keeps 2～4 hours；Afterwards by catalyst 600
DEG C calcining；Thus obtain preliminary catalytic agent, catalyst needs to use Hydrogen activation in the reactor before use；
The precursor of described primary catalyst metal is co (no3)2·6h2o；The precursor of described promoter metal is selected from
nh4reo4、rucl3·3h2o、cu(no3)2·3h2o、mg(no3)2·6h2o、zr(no3)4·5h2O and h2ptcl6·6h2In o
One kind or any two kinds.
Being preferably in combination with of catalyst:
co(no3)2·6h2o/rucl3·3h2o/zr(no3)4·5h2(weight is than preferably 1:0.002- for o/ carrier
0.003:0.8-0.9:1.8-2.2, for example, 1:0.0026:0.86:2)；
co(no3)2·6h2o/rucl3·3h2o/zr(no3)4·5h2(weight is than preferably 1:0.002- for o/ carrier
0.003:0.8-0.9:1.8-2.2, for example, 1:0.0026:0.86:2)；
co(no3)2·6h2o/nh4reo4/zr(no3)4·5h2O/ carrier (weight is than preferably 1:0.002-0.004:
0.8-0.9:1.8-2.2, for example, 1:0.0029:0.86:2)；
co(no3)2·6h2o/cu(no3)2·3h2o/mg(no3)2·6h2O/ carrier (weight is than preferably 1:0.3-0.5:
0.04-0.06:1.8-2.2, for example, 1:0.38:0.05:2)；
co(no3)2·6h2o/h2ptcl6·6h2O/ carrier is (weight than preferably 1:0.05-0.06:1.8-2.2, for example
For 1:0.053:2).
It is 500m that described carrier is preferably specific surface area2/ g smog sio2.
Described catalyst was preferably 3～6 hours in the time of 600 DEG C of calcinings.
Preferably, described stirring is to utilize magnetic stirrer, and the rotating speed of described magnetic stirrer is 1000rpm/
min.
Preferably, the consumption of described catalyst and the ratio of the airflow rate of synthesis gas are 5g:60～120ml/min,
Catalyst 80 mesh glass dust using same volume in fixed bed are diluted.
Preferably, 1atm Hydrogen activation directly used before the reaction in fixed bed reactors by described catalyst.
Preferably, the temperature of described Hydrogen activation is 400 DEG C；Time is 4～8 hours, hydrogen flow rate 90ml/min.
Preferably, described biomass synthesis gas are converted into the combustion of alkane liquid in the fixed bed reactors be filled with catalyst
The reaction temperature of material is 180～230 DEG C.
Preferably, described synthesis atmospheric pressure is 0.1～1.0mpa.
The invention provides a kind of effective way by renewable raw materials synthetic engine fuel.Have the advantage that
1. the method for the present invention is simple, does not have the process of complexity, the either preparation of catalyst, or follow-up reaction is all
Fairly simple, it is suitable for industrial needs；
2. the product that the present invention obtains is the liquid fuel based on long chain alkane, and this fuel oil product can be directly used as liquid
Fluid fuel or be used in mixed way with existing fuel.
3. the catalyst system of the present invention, the characteristics design for biomass synthesis gas and preparation, and show very high
Activity and stability.
Specific embodiment
The present invention is turned by the catalysis that fischer-tropsch reaction obtains alkane liquid fuel by biomass synthesis gas
A kind of specific embodiment of the method changed is: 5.0g Catalyst packing in fixed bed reaction, adopt in fixed bed by catalyst
It is diluted with 80 mesh glass dust of same volume, fixed bed reaction pipe is by heating by electric cooker.Catalyst is anti-in fixed bed before the reaction
Answer in device and directly use 1.0atm Hydrogen activation, activation temperature is 400 DEG C, the time is 4～8 hours, hydrogen flow rate 90ml/min.Live
After change, in the hydrogen gas stream the temperature of catalyst is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.Reaction temperature
180～230 DEG C, synthesize atmospheric pressure 0.1～1.0mpa, airflow rate 60～120ml/min.Product is collected by water-cooled.
Described catalyst is formed by the primary catalyst metal of supported on carriers and co-catalysis metal, wherein main catalytic
The load capacity of agent metal is 10～20wt% of vehicle weight；Described promoter metal and described primary catalyst metal
The mass values of material are 0.01～2.0；
Described primary catalyst metal is cobalt, and described promoter metal is selected from re, ru, cu, mg, zr or pt one
Plant or any two kinds.
Described catalyst is prepared by following methods:
The precursor of the precursor of the primary catalyst metal of 5.0～9.9g and the promoter metal of 0.01～5.0g is dissolved in
In 150ml deionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring (magnetic
Property stirrer rotating speed be 1000rpm/min) under add heat of solution in, continue heating (90 DEG C) stirring (magnetic stirrer turn
Speed is 1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated in atmosphere
To 300 DEG C and keep 3 hours；Afterwards catalyst is calcined 3～6 hours at 600 DEG C；Thus obtain preliminary catalytic agent, catalyst
Need before use to use Hydrogen activation in the reactor.
The precursor of described primary catalyst metal is co (no3)2·6h2o；The precursor of described promoter metal is selected from
nh4reo4、rucl3·3h2o、cu(no3)2·3h2o、mg(no3)2·6h2o、zr(no3)4·5h2O and h2ptcl6·6h2In o
One kind or any two kinds.
For a better understanding of the present invention, it is further elucidated with present disclosure with reference to specific embodiment, but this
Bright it is not construed as being limited only to the following examples.
Embodiment 1
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2The rucl of o, 0.013g3·3h2O and 4.3g zr (no3)4·5h2O is dissolved in 150ml
In deionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring, (magnetic is stirred
The rotating speed mixing son is 1000rpm/min) under add in heat of solution, (rotating speed of magnetic stirrer is to continue (90 DEG C) stirrings of heating
1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated to 300 in atmosphere
DEG C and keep 3 hours；Afterwards catalyst is calcined 3 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 8 hours, hydrogen flow rate 90ml/min.After activation, in the hydrogen gas stream by catalyst
Temperature is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.230 DEG C of reaction temperature, synthesizes atmospheric pressure 1.0mpa, gas
Flow velocity rate 120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is distributed as c according to carbon number5~
c615.1%, c7～c955.2%, c10～c2029.7%.The efficiency of carbon con version of biomass synthesis gas is 83.5%.
Substantially adopt above-mentioned identical method, simply prepare the co (no in catalyst3)2·6h2o、rucl3·3h2O and
zr(no3)4·5h2The content of o is different, the method that products therefrom adopts above-mentioned product analysis, and result is as shown in table 1.
Table 1
Embodiment 2
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2The rucl of o, 0.013g3·3h2O and 4.3g zr (no3)4·5h2O is dissolved in 150ml
In deionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring, (magnetic is stirred
The rotating speed mixing son is 1000rpm/min) under add in heat of solution, (rotating speed of magnetic stirrer is to continue (90 DEG C) stirrings of heating
1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated to 300 in atmosphere
DEG C and keep 3 hours；Afterwards catalyst is calcined 3～6 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 4～8 hours, hydrogen flow rate 90ml/min.After activation, will be catalyzed in the hydrogen gas stream
The temperature of agent is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.230 DEG C of reaction temperature, synthesizes atmospheric pressure
1.0mpa, airflow rate 120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is according to the distribution of carbon number.
Substantially adopt above-mentioned identical method, the treatment conditions simply prepared during catalyst are different, and products therefrom adopts
The method of above-mentioned product analysis, result is as shown in table 2.
Table 2
Embodiment 3
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2The rucl of o, 0.013g3·3h2O and 4.3g zr (no3)4·5h2O is dissolved in 150ml
In deionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring, (magnetic is stirred
The rotating speed mixing son is 1000rpm/min) under add in heat of solution, (rotating speed of magnetic stirrer is to continue (90 DEG C) stirrings of heating
1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated to 300 in atmosphere
DEG C and keep 3 hours；Afterwards catalyst is calcined 3 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 8 hours, hydrogen flow rate 90ml/min.After activation, in the hydrogen gas stream by catalyst
Temperature is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.180～230 DEG C of reaction temperature, synthesizes atmospheric pressure 0.1
～1.0mpa, airflow rate 60～120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is according to the distribution of carbon number.
Substantially adopt above-mentioned identical method, simply prepare Catalyst Testing Conditions difference, products therefrom adopts above-mentioned
The method of product analysis, result is as shown in table 3.
Table 3
Embodiment 4
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2The nh of o, 0.0144g4reo4With 4.3g zr (no3)4·5h2O is dissolved in 150ml and goes
In ionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring (magnetic stirring
The rotating speed of son is 1000rpm/min) under add in heat of solution, (rotating speed of magnetic stirrer is to continue (90 DEG C) stirrings of heating
1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated to 300 in atmosphere
DEG C and keep 3 hours；Afterwards catalyst is calcined 3 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 8 hours, hydrogen flow rate 90ml/min.After activation, in the hydrogen gas stream by catalyst
Temperature is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.230 DEG C of reaction temperature, synthesizes atmospheric pressure 1.0mpa, gas
Flow velocity rate 120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is distributed as c according to carbon number5~
c614.3%, c7～c954.1%, c10～c2031.6%.The efficiency of carbon con version of biomass synthesis gas is 86.7%.
Substantially adopt above-mentioned identical method, simply prepare the co (no in catalyst3)2·6h2o、nh4reo4And zr
(no3)4·5h2The content of o is different, the method that products therefrom adopts above-mentioned product analysis, and result is as shown in table 4.
Table 4
Embodiment 5
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2Cu (the no of o, 1.9g3)2·3h2O and 0.25g mg (no3)2·6h2O is dissolved in
In 150ml deionized water, it is heated to 90 DEG C.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring (magnetic
Property stirrer rotating speed be 1000rpm/min) under add heat of solution in, continue heating (90 DEG C) stirring (magnetic stirrer turn
Speed is 1000rpm/min) to carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated in atmosphere
To 300 DEG C and keep 3 hours；Afterwards catalyst is calcined 3 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 8 hours, hydrogen flow rate 90ml/min.After activation, in the hydrogen gas stream by catalyst
Temperature is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.230 DEG C of reaction temperature, synthesizes atmospheric pressure 1.0mpa, gas
Flow velocity rate 120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is distributed as c according to carbon number5~
c616.4%, c7～c943.7%, c10～c2040.6%.The efficiency of carbon con version of biomass synthesis gas is 68.4%.
Substantially adopt above-mentioned identical method, simply prepare the co (no in catalyst3)2·6h2o、cu(no3)2·
3h2O and mg (no3)2·6h2The content of o is different, the method that products therefrom adopts above-mentioned product analysis, and result is as shown in table 5.
Table 5
Embodiment 6
(1) preparation of catalyst
Co (no by 5.0g3)2·6h2The h of o and 0.265g2ptcl6·6h2O is dissolved in 150ml deionized water, is heated to
90℃.(specific surface area is 500m to the carrier of 10.0g2/ g smog sio2) in quick stirring, (rotating speed of magnetic stirrer is
Add under 1000rpm/min) in heat of solution, continue (90 DEG C) stirrings of heating (rotating speed of magnetic stirrer is 1000rpm/min)
To carrier dried, obtain catalyst precarsor, then again gained catalyst precarsor is heated to 300 DEG C in atmosphere and keeps 3 little
When；Afterwards catalyst is calcined 3 hours at 600 DEG C.
(2) fixed bed reaction
In fixed bed reaction, catalyst 80 mesh glass dust using same volume in fixed bed enter 5.0g Catalyst packing
Row dilution, fixed bed reaction pipe is by heating by electric cooker.1.0atm hydrogen directly used before the reaction in fixed bed reactors by catalyst
Activation, activation temperature is 400 DEG C, and the time is 8 hours, hydrogen flow rate 90ml/min.After activation, in the hydrogen gas stream by catalyst
Temperature is down to reaction temperature, and hydrogen stream is switched to reacting synthesis gas.230 DEG C of reaction temperature, synthesizes atmospheric pressure 1.0mpa, gas
Flow velocity rate 120ml/min.Product is collected by water-cooled.
(3) product analysis
Liquid product is analyzed by gc-ms, and product is mainly alkane, and it is distributed as c according to carbon number5~
c621.3%, c7～c954.5%, c10～c2024.3%.The efficiency of carbon con version of biomass synthesis gas is 89.7%.
Substantially adopt above-mentioned identical method, simply prepare the co (no in catalyst3)2·6h2O and h2ptcl6·
6h2The content of o is different, the method that products therefrom adopts above-mentioned product analysis, and result is as shown in table 6.
Table 6
The above-mentioned specific embodiment technical scheme that the invention is not limited in any way, every using equivalent or wait
The technical scheme that the mode of effect conversion is obtained all falls within protection scope of the present invention.
Claims (9)
1. a kind of method biomass synthesis gas being converted into liquid fuel by fischer-tropsch reaction, is characterized in that:
Biomass synthesis gas are converted into alkane liquid fuel, described alkane liquid fuel in the fixed bed reactors be filled with catalyst
Collected by direct water-cooling；
Described catalyst is formed by the primary catalyst metal of supported on carriers and co-catalysis metal, wherein major catalyst gold
The load capacity belonging to is the 10～20% of vehicle weight；Described promoter metal and the material of described primary catalyst metal
Mass values are 0.01～2.0；Described primary catalyst metal is cobalt, described promoter metal be selected from re, ru, cu, mg,
Two kinds of one of zr and pt or any,
Described catalyst is prepared by following methods:
Before the promoter metal of the precursor of the primary catalyst metal of 5.0～9.9 weight portions and 0.0265～5.0 weight portion
Body is dissolved in 150 parts by volume deionized waters, is heated to seething with excitement；The carrier of 10 weight portions adds in heat of solution under fast stirring,
Continue heating stirring to carrier dried, obtain catalyst precarsor, wherein, described weight portion: described parts by volume=gram: milliliter, so
Again gained catalyst precarsor is heated to 300 DEG C in atmosphere afterwards and keeps 2～4 hours；Afterwards catalyst is forged at 600 DEG C
Burn；Thus obtain preliminary catalytic agent, catalyst needs to use Hydrogen activation in the reactor before use；
The precursor of described primary catalyst metal is co (no3)2·6h2o；The precursor of described promoter metal is selected from
nh4reo4、rucl3·3h2o、cu(no3)2·3h2o、mg(no3)2·6h2o、zr(no3)4·5h2O and h2ptcl6·6h2In o
One kind.
2. method according to claim 1, is characterized in that: described carrier is specific surface area is 500m2/ g smog sio2.
3. method according to claim 1, is characterized in that: described catalyst is little for 3～6 in the time of 600 DEG C of calcinings
When.
4. method according to claim 1, is characterized in that: described stirring is to utilize magnetic stirrer, described magnetic
The rotating speed of stirrer is 1000rpm/min.
5. method according to claim 1, is characterized in that: the consumption of described catalyst and the airflow rate of synthesis gas
Ratio is 5g:60～120ml/min, and catalyst 80 mesh glass dust using same volume in fixed bed are diluted.
6. method according to claim 1, is characterized in that: described catalyst is straight in fixed bed reactors before the reaction
Connect and use 1atm Hydrogen activation.
7. method according to claim 6, is characterized in that: the temperature of described Hydrogen activation is 400 DEG C；Time is little for 4～8
When, hydrogen flow rate 90ml/min.
8. method according to claim 1, is characterized in that: described biomass synthesis gas are being filled with the fixed bed of catalyst
The reaction temperature being converted into alkane liquid fuel in reactor is 180～230 DEG C.
9. method according to claim 1, is characterized in that: described synthesis atmospheric pressure is 0.1～1.0mpa.
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| CN101168679A (en) * | 2007-12-06 | 2008-04-30 | 四川大学 | Method for preparing liquid fuel by using biomass material |
| CN101966463A (en) * | 2010-09-08 | 2011-02-09 | 陕西师范大学 | Cobalt-based catalyst for controlling distribution of Fisher-Tropsch synthetic products and application thereof |
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| CN102869752A (en) * | 2011-04-01 | 2013-01-09 | 韩国能量技术研究院 | 2-stage F-T reactor system for increasing conversion rate of synthesis gas |
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| CN101168679A (en) * | 2007-12-06 | 2008-04-30 | 四川大学 | Method for preparing liquid fuel by using biomass material |
| CN102304380A (en) * | 2010-07-23 | 2012-01-04 | 中国科学技术大学 | Method for preparing biomass-based mixed liquid fuel from biomass and bio oil |
| CN101966463A (en) * | 2010-09-08 | 2011-02-09 | 陕西师范大学 | Cobalt-based catalyst for controlling distribution of Fisher-Tropsch synthetic products and application thereof |
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