CN101195088A - Catalyst for synthesizing gas and liquid fuel, preparation method and application thereof - Google Patents
Catalyst for synthesizing gas and liquid fuel, preparation method and application thereof Download PDFInfo
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- CN101195088A CN101195088A CNA2007101728622A CN200710172862A CN101195088A CN 101195088 A CN101195088 A CN 101195088A CN A2007101728622 A CNA2007101728622 A CN A2007101728622A CN 200710172862 A CN200710172862 A CN 200710172862A CN 101195088 A CN101195088 A CN 101195088A
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Abstract
The invention relates to a catalyst which is used for synthesis gas and synthetic fluid fuel, a process for preparation and use. The catalyst is composed of three parts of active components, additives and carriers, wherein the active components are iron and cobalt, the metallic iron and the cobalt account for 5%-30% of the total weight of the catalyst, the additives are zirconium and potassium, potassium additive accounts for 0.01%-15% of the total weight of the catalyst, zirconium additive accounts for 1%-20% of the total weight of the catalyst, and the others are the carriers. Compared with the prior art, the catalyst of the invention has comparatively high hydrogenation activity to CO and comparatively high selectivity and receiving rate to C5+.
Description
Technical field
The present invention relates to a kind of Fischer-Tropsch synthesis catalyst, it relates to a kind of catalyst and preparation method and purposes that is used for the synthesis gas synthetic liquid fuel.
Background technology
Fischer-Tropsch synthetic (it is synthetic to be called for short F-T) is meant synthesis gas (CO+H
2) on catalyst, transforming the reaction that generates hydro carbons, product comprises various alkane and alkene, and by-product CO
2And H
2Organic oxygen-containing compounds such as O and alcohol, aldehyde, ketone, acid and ester, product can get high-quality liquid fuel such as gasoline, diesel oil, aviation kerosine etc. through deep processing.
China is the country of a rapid economic development, the demand of the energy and day sharp increase, oneself jeopardizes the economic and national security of China the imbalance between supply and demand of oil product resource, Fischer-Tropsch synthetic mainly is made up of linear paraffin, alkene in addition, have characteristics such as no sulphur, no nitrogen, no metal, nothing or minute quantity aromatic hydrocarbons, it is environment amenable liquid fuel, the F-T synthetic technology that development coal/natural gas is produced oil product has very important significance, and wherein catalyst development is that this process realizes one of industrialized committed step.
Fe and Co are adopted in the research and development of Fischer-Tropsch synthetic catalyst more.Fe Catalyst for CO hydrogenation activity is higher, but under reaction condition, the easy oxidation of Fe, carbon deposit, active high to water gas shift reaction in addition, the chain growth ability of synthetic hydrocarbon.And Co is insensitive to water gas reaction, the catalytic hydrogenation activity height, and reaction rate is not subjected to the influence of water partial pressure, is difficult for carbon deposit and poisoning, and generates CO
2The selectivity height of low, the long chain hydrocarbon of selectivity, oxygenatedchemicals is less etc. in the product, is considered to synthetic at present long chain hydrocarbon catalyst system preferably.
Fe, Co be simultaneously as the activity of such catalysts component, have that non-Fe, Co simply add and good property.(Appl.Catal A:Gen.1997 153:43) has reported that F-T synthesizes at reaction temperature 493K, pressure 1MPa, air speed 350h to document
-1, H
2Under the operating condition of/CO=2,10%Co/TiO
2, 10%Fe10%Co/TiO
2And 10%Fe/TiO
2The conversion ratio of CO is respectively 36.0%, 19.7%, 7.7% on the catalyst, CH
4Selectivity be followed successively by 14.5%, 8.0%, 5.4%, (React.Kinetic.Catalysis Letter such as Sergio L Gonz á lez-Cort é s, 2002,75:3) studied manganese modification ferrum-cobalt catalyst, discover the good stability of this catalyst than the ferrimanganic catalyst.For SiO
2The Co catalysts of load, ZrO
2Be a kind of good F-T synthesis accelerant, find Co and SiO
2The surface compound (reduction temperature is more than the 800K) that forms cobaltous silicate and so on added ZrO before carrier is flooding Co
2The time, zirconium can be at SiO
2Protective layer of last formation, thus Co and SiO stoped
2Form the surface compound of cobaltous silicate and so on; Potassium promoter is one of co-catalyst during the maximum F-T of application synthesizes.In Fe was catalyst based, K can promote the generation of alkene, heavy hydrocarbon, suppressed methane, therefore the application of K in Fe is catalyst based is more extensive, and K influences cobalt-base catalyst, discovers that K can improve catalyst surface C/H ratio, the generation of favourable heavy hydrocarbon, the while can be reduced the output of methane.
Do not see as yet that at present domestic iron, cobalt are active component, potassium or zirconium are auxiliary agent, the report of fischer-tropsch synthetic catalyst.
Summary of the invention
Purpose of the present invention is exactly to provide a kind of for the defective that overcomes above-mentioned prior art existence CO to be had higher hydrogenation activity, C
5 +The catalyst that is used for the synthesis gas synthetic liquid fuel and preparation method and purposes with higher selectivity and yield.
Purpose of the present invention can be achieved through the following technical solutions: a kind of catalyst that is used for the synthesis gas synthetic liquid fuel, it is characterized in that, this catalyst is made up of active component, auxiliary agent and carrier three parts, described active component is iron and cobalt, metallic iron and cobalt account for 5～30% of total catalyst weight, and described auxiliary agent is zirconium or potassium, and potassium promoter accounts for 0.01～15% of total catalyst weight, the zirconium auxiliary agent accounts for 1～20% of total catalyst weight, and all the other are carrier.
The weight ratio of metallic iron and cobalt is 1: 0.5～5 in the described active component.
Described carrier is selected silica gel for use, and the specific area of this silica gel is 200～400m
2/ g, average pore volume is 0.2～1ml/g, pore-size distribution is at 4～10nm.
A kind of Preparation of catalysts method that is used for the synthesis gas synthetic liquid fuel, it is characterized in that, with 5～30% (weight) iron, cobalt active component, the solution impregnating carrier of the nitrate of auxiliary agent potassium 0.01～15% (weight) or zirconium 1～20% (weight), static ageing, drying, roasting, use hydrogen reducing, reduction temperature is 100～800 ℃, 1～80 hour recovery time.
Described carrier is selected silica gel for use, and the specific area of this silica gel is 200～400m2/g, and average pore volume is 0.2～1ml/g, and pore-size distribution is at 4～10nm.
A kind of purposes that is used for the catalyst of synthesis gas synthetic liquid fuel is characterized in that, catalyst is reduced with hydrogen, and reduction temperature is 220～500 ℃, and pressure is 0.3～2MPa, and air speed is 300～2000h
-1(V/V), carry out Fischer-Tropsch synthesis then, reaction condition is: 220～400 ℃ of temperature, pressure 0.5～5MPa, air speed 300～2000h
-1(V/V).
Catalyst of the present invention is made up of active component, auxiliary agent and carrier three parts, and active component is iron, cobalt, and auxiliary agent is zirconium, potassium, and as the zirconium auxiliary agent, addition is 1～20%, is higher than at 20% o'clock, and activity of such catalysts changes not obvious; As potassium promoter, addition is 0.01～20%, is higher than at 15% o'clock, and activity of such catalysts descends.Compared with prior art, use catalyst of the present invention to carry out Fischer-Tropsch synthesis, CO has high conversion ratio, C
5 +Have higher selectivity and yield.
The specific embodiment
The invention will be further described below in conjunction with the specific embodiment.
Embodiment 1.
Take by weighing silica-gel carrier 10g, configuration 9.04 gram Fe (NO
3)
39H
2O, 6.17 gram Co (NO
3)
26H
2The aqueous solution 9.62ml of O, the still aging 24h of dipping under the room temperature, behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h obtain 10%Fe10%Co/SiO
2(percetage by weight, down together) catalyst 1.
Embodiment 2.
Take by weighing silica-gel carrier 12g, configuration 6.20 gram Fe (NO
3)
39H
2O, 7.05 gram Co (NO
3)
26H
2The aqueous solution 11.55ml of O, the still aging 24h of dipping under the room temperature, behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h obtain 6%Fe10%Co/SiO
2Catalyst 2.
Embodiment 3.
Take by weighing silica-gel carrier 12g, configuration 1.97 gram Fe (NO
3)
39H
2O, 6.93 gram Co (NO
3)
26H
2The aqueous solution 11.55ml of O, the still aging 24h of dipping under the room temperature, behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h obtain 2%Fe10%Co/SiO
2Catalyst 3.
Embodiment 4.
Take by weighing silica-gel carrier 12g, configuration 1.99 gram Fe (NO
3)
39H
2O, 6.81 gram Co (NO
3)
26H
2O, 0.65 gram Zr (NO
3)
45H
2The aqueous solution 11.55ml of O, the still aging 24h of dipping under the room temperature, behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h obtain 2%Fe10%Co1%Zr/SiO
2Catalyst 4.
Embodiment 5.
Take by weighing silica-gel carrier 12g, configuration 3.40 gram Zr (NO3) 45H
2The aqueous solution of O floods, and behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h dispose 1.99 gram Fe (NO then
3)
39H
2O, 6.81 gram Co (NO3) 26H
2O aqueous solution 11.55m, the still aging 24h of dipping under the room temperature, behind 80 ℃ of following dry 8h, 400 ℃ of following roasting 6h obtain 2%Fe10%Co5%Zr/SiO
2Catalyst 5.
Embodiment 6.
Take by weighing silica-gel carrier 12g, configuration 1.99 gram Fe (NO
3)
39H
2O, 6.81 gram Co (NO
3)
26H
2O, 0.018 gram KNO
3Aqueous solution 11.55ml, the still aging 24h of dipping under the room temperature, 80 ℃ down behind the dry 8h, 400 ℃ of following roasting 6h obtain 2%Fe10%Co0.05%K/SiO
2Catalyst 6.
Embodiment 7.
Take by weighing silica-gel carrier 12g, configuration 1.99 gram Fe (NO
3)
39H
2O, 6.81 gram Co (NO
3)
26H
2O, 0.04 gram KNO
3Aqueous solution 11.55ml, the still aging 24h of dipping under the room temperature, 80 ℃ down behind the dry 8h, 400 ℃ of following roasting 6h obtain, and obtain 2%Fe10%Co0.1%K/SiO
2Catalyst 7.
Embodiment 8.
Get 20～40 order catalyst 3ml in the example 1, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 250 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 9.
Get 20～40 order catalyst 3ml in the example 2, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 250 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 10.
Get 20～40 order catalyst 3ml in the example 3, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 250 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 11.
Get 20～40 order catalyst 3ml in the example 4, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 230 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 12.
Get 20～40 order catalyst 3ml in the example 5, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 230 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 13.
Get 20～40 order catalyst 3ml in the example 6, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 230 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Embodiment 14.
Get 20～40 order catalyst 3ml in the example 7, be seated in the flat-temperature zone of fixed bed reactors after the quartz sand dilution with same particle sizes, hydrogen reducing, air speed is 1500h
-1, pressure is 0.5MPa, slowly is warmed up to 420 ℃ by 200 ℃, heating rate is 0.5 ℃/min, at 420 ℃ of following constant temperature 6h, cool to 200 ℃ in atmosphere of hydrogen afterwards then, be converted to synthesis gas, heating rate with 0.5 ℃/min is warmed up to 230 ℃, and conditioned reaction pressure is 1MPa, air speed 600h
-1, H
2/ CO=1.6 more than the reaction 20h, carries out analytical test.
Table 1 experimental result
| Catalyst | Reaction condition | X CO/％ | S CH4/％ | C 5 +/％ | Y 5+/gm -3 |
| Embodiment 8 | 250℃，1MPa，600h -1， | 77.67 | 10.11 | 68.19 | 114.85 |
| H 2/CO＝1.6 | |||||
| Embodiment 9 | 250℃，1MPa，600h -1， H 2/CO＝1.6 | 82.00 | 11.48 | 66.23 | 119.81 |
| Embodiment 10 | 250℃，1MPa，600h -1， H 2/CO＝1.6 | 92.99 | 12.13 | 57.63 | 117.11 |
| Embodiment 11 | 230℃，1MPa，600h -1， H 2/CO＝1.6 | 64.74 | 9.51 | 78.42 | 113.62 |
| Embodiment 12 | 230℃，1MPa，600h -1， H 2/CO＝1.6 | 95.08 | 11.91 | 75.05 | 155.21 |
| Embodiment 13 | 230℃，1MPa，600h -1， H 2/CO＝1.6 | 62.02 | 8.64 | 81.84 | 112.51 |
| Embodiment 14 | 230℃，1MPa，600h -1， H 2/CO＝1.6 | 44.03 | 10.1 | 79.61 | 77.65 |
Embodiment 15
With Fe (NO
3)
39H
2O, Co (NO
3)
26H
2O, Zr (NO
3)
45H
2O is the feedstock production catalyst, makes metallic iron and cobalt account for 5% of total catalyst weight, and zirconium accounts for 1% of total catalyst weight, is carrier with silica gel, and the specific area of this silica gel is 200m
2/ g, average pore volume is 0.2ml/g, pore-size distribution is at 4nm.Obtain 2%Fe3%Co1%Zr/SiO
2Catalyst is used hydrogen reducing 1 hour down at 100 ℃, carries out Fischer-Tropsch synthesis then, and reaction condition is: 220 ℃ of temperature, pressure 0.5MPa, air speed 300h
-1(V/V).
Embodiment 16
With Fe (NO
3)
39H
2O, Co (NO
3)
26H
2O, Zr (NO
3)
45H
2O is the feedstock production catalyst, makes metallic iron and cobalt account for 30% of total catalyst weight, and zirconium accounts for 20% of total catalyst weight, is carrier with silica gel, and the specific area of this silica gel is 400m
2/ g, average pore volume is 1ml/g, pore-size distribution is at 10nm.Obtain 10%Fe20%Co20%Zr/SiO
2Catalyst is used hydrogen reducing 80 hours down at 800 ℃, carries out Fischer-Tropsch synthesis then, and reaction condition is: 400 ℃ of temperature, pressure 2MPa, air speed 2000h
-1(V/V).
Embodiment 17
With Fe (NO
3)
39H
2O, Co (NO
3)
26H
2O, KNO
3The aqueous solution be the feedstock production catalyst, make metallic iron and cobalt account for 5% of total catalyst weight, potassium accounts for 0.01% of total catalyst weight, is carrier with silica gel, the specific area of this silica gel is 200m
2/ g, average pore volume is 0.2ml/g, pore-size distribution is at 4nm.Obtain 2%Fe3%Co0.01%K/SiO
2Catalyst is 300h with air speed under 220 ℃, 0.3MPa
-1(V/V) hydrogen reducing 1 hour carries out Fischer-Tropsch synthesis then, and reaction condition is: 220 ℃ of temperature, pressure 0.5MPa, air speed 300h
-1(V/V).
Embodiment 18
With Fe (NO
3)
39H
2O, Co (NO
3)
26H
2O, KNO
3The aqueous solution be the feedstock production catalyst, make metallic iron and cobalt account for 30% of total catalyst weight, potassium accounts for 15% of total catalyst weight, is carrier with silica gel, the specific area of this silica gel is 400m
2/ g, average pore volume is 1ml/g, pore-size distribution is at 10nm.Obtain 10%Fe20%Co15%K/SiO
2Catalyst is 2000h with air speed under 500 ℃, 2MPa
-1(V/V) hydrogen reducing 80 hours carries out Fischer-Tropsch synthesis then, and reaction condition is: 400 ℃ of temperature, pressure 2MPa, air speed 2000h
-1(V/V).
As can be seen from the above-described embodiment, adopting K or Zr is the described catalyst of auxiliary agent when carrying out Fischer-Tropsch synthesis, and CO is had high conversion ratio, C
5 +Have higher selectivity and yield.
Claims (6)
1. catalyst that is used for the synthesis gas synthetic liquid fuel, it is characterized in that, this catalyst is made up of active component, auxiliary agent and carrier three parts, described active component is iron and cobalt, metallic iron and cobalt account for 5～30% of total catalyst weight, and described auxiliary agent is zirconium or potassium, and potassium promoter accounts for 0.01～15% of total catalyst weight, the zirconium auxiliary agent accounts for 1～20% of total catalyst weight, and all the other are carrier.
2. a kind of catalyst that is used for the synthesis gas synthetic liquid fuel according to claim 1 is characterized in that the weight ratio of metallic iron and cobalt is 1: 0.5～5 in the described active component.
3. a kind of catalyst that is used for the synthesis gas synthetic liquid fuel according to claim 1 is characterized in that described carrier is selected silica gel for use, and the specific area of this silica gel is 200～400m
2/ g, average pore volume is 0.2～1ml/g, pore-size distribution is at 4～10nm.
4. described Preparation of catalysts method that is used for the synthesis gas synthetic liquid fuel of claim 1, it is characterized in that, with 5～30% (weight) iron, cobalt active component, the solution impregnating carrier of the nitrate of auxiliary agent potassium 0.01～15% (weight) or zirconium 1～20% (weight), static ageing, drying, roasting, use hydrogen reducing, reduction temperature is 100～800 ℃, 1～80 hour recovery time.
5. a kind of Preparation of catalysts method that is used for the synthesis gas synthetic liquid fuel according to claim 4 is characterized in that described carrier is selected silica gel for use, and the specific area of this silica gel is 200～400m
2/ g, average pore volume is 0.2～1ml/g, pore-size distribution is at 4～10nm.
6. the described purposes that is used for the catalyst of synthesis gas synthetic liquid fuel of claim 1 is characterized in that, catalyst is reduced with hydrogen, and reduction temperature is 220～500 ℃, and pressure is 0.3～2MPa, and air speed is 300～2000h
-1(V/V), carry out Fischer-Tropsch synthesis then, reaction condition is: 220～400 ℃ of temperature, pressure 0.5～5MPa, air speed 300～2000h
-1(V/V).
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|---|---|---|---|
| CNA2007101728622A CN101195088A (en) | 2007-12-24 | 2007-12-24 | Catalyst for synthesizing gas and liquid fuel, preparation method and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101728622A CN101195088A (en) | 2007-12-24 | 2007-12-24 | Catalyst for synthesizing gas and liquid fuel, preparation method and application thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101195088A true CN101195088A (en) | 2008-06-11 |
Family
ID=39545825
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|---|---|---|---|
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Country Status (1)
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104588023A (en) * | 2013-11-01 | 2015-05-06 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis catalyst, and preparation method and application thereof |
| CN108067235A (en) * | 2016-11-15 | 2018-05-25 | 中国科学院大连化学物理研究所 | A kind of catalyst of synthesis gas alkene coproduction higher alcohols and its preparation and application |
-
2007
- 2007-12-24 CN CNA2007101728622A patent/CN101195088A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104588023A (en) * | 2013-11-01 | 2015-05-06 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis catalyst, and preparation method and application thereof |
| CN108067235A (en) * | 2016-11-15 | 2018-05-25 | 中国科学院大连化学物理研究所 | A kind of catalyst of synthesis gas alkene coproduction higher alcohols and its preparation and application |
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Open date: 20080611 |