CN103695022A - Fischer-Tropsch synthesis process applicable to fixed-bed reactor - Google Patents
Fischer-Tropsch synthesis process applicable to fixed-bed reactor Download PDFInfo
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Abstract
The invention relates to a Fischer-Tropsch synthesis process applicable to a fixed-bed reactor. The process comprises the steps of dividing a bed layer into an upper section, a middle section and a lower section, loading a diluted catalyst, and enabling a circulating medium to enter the catalyst bed layer after the circulating medium is preheated; preheating raw material gas which is formed by mixing fresh synthesis gas and recycling gas, then enabling the preheated raw material gas to enter the catalyst bed layer for Fischer-Tropsch synthesis reaction, carrying out oil-gas-water three-phase separation on a reaction product, carrying out wastewater treatment on separated synthesis water, taking one part of the separated gas as purge gas, converging the other part of the separated gas and the fresh synthesis gas, and taking mixed gas as the raw material gas; separating the separated liquid, taking one part of C5-C8 obtained through separating as the circulating medium, and taking the rest of C5-C8 for other purposes. The process has the advantages of high heat exchange efficiency, uniform bed layer temperature, stability in operation and easiness in control.
Description
Technical field
The present invention relates to a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor.
Technical background
Coal is produced oil fuel and chemical is one of the important content in clean coal technology field through Fischer-Tropsch is synthetic.Now, fluidized-bed, slurry state bed and fixed-bed reactor are principal reaction devices of Fischer-Tropsch synthesis.Although fluidized-bed reactor heat transfer coefficient is high, heat-transfer effect good, is easy to automatic production, its fluid mapper process is restive, and catalyst utilization is low, back-mixing, serious wear; Although paste state bed reactor temperature of reaction is even, productive rate is high, also has serious back-mixing, and the separation of catalyzer is also an insoluble problem; There is the poor feature of the even bed thermal conductivity of bed temperature skewness in fixed-bed reactor, but fixed-bed reactor volume is little, and catalyzer loading amount is little, is suitable for High Temperature High Pressure operation, thereby is usually used in Fischer-Tropsch synthesis process.Cobalt-base catalyst particularly, it has high reactivity, high stability, low water gas shift reaction, low methane selectively, high C
5 +the advantages such as selectivity.But cobalt catalyst cost is higher, problem separated and that run off causes it not to be suitable for slurry state bed and fluidized-bed reactor, and the fixed-bed reactor that are applied to preferably.But cobalt catalyst causes it can not industrial applications for fixed bed exists two problems, the firstth, reaction bed temperature is uneven, very easily temperature runaway; The secondth, temperature inequality causes bed utilization ratio low, and productive rate is low.
The original intention of fixed-bed reactor design is exactly mainly with the form of the evaporation of water latent heat of vaporization, to take away the amount of heat producing in reaction tubes.Boiled water is by heat exchange between pipe, and by-product high-pressure steam, has strengthened heat transfer process.But existing technique still cannot effectively remove the large calorimetric that fischer-tropsch reaction is emitted, still there is the problem of beds temperature runaway.Since fixed bed can dispel the heat by the latent heat of vaporization between pipe, so also it can strengthen conducting heat by the latent heat of vaporization effect in pipe, and just urgently exploitation is a kind of so at present can effectively move hot Fischer-Tropsch synthesis process in managing.
Summary of the invention
The invention provides that a kind of heat exchange efficiency is high, bed temperature evenly, the fixed bed reaction technique for Fischer-Tropsch synthesis controlled of stable operation being easy to.
Fischer-Tropsch synthesis process of the present invention adopts ferrum-based catalyst or cobalt-base catalyst, is preferably longer cobalt-base catalyst of life-span.Described beds can be unanimous between the higher and lower levels, can be also according to bed hotspot's distribution, with thinner, presses different ratios dilution filling, and the temperature that can realize better so whole reaction bed is even, makes advantage of the present invention more outstanding.
The present invention specifically realizes by following steps:
(1) bed is divided into upper, middle and lower segment, the catalyzer that need to load three bed sections, fills out than for 0-1:1 dilutes laggard luggage by thinner and catalyst volume;
(2) circulatory mediator is preheated to after the temperature of supercritical state under reaction pressure, from the top of fixed-bed reactor, enters beds;
(3) fresh synthesis gas and circulation gas enter beds from fixed-bed reactor upper feeding mouth separately after being mixed to form unstripped gas preheating, or from fixed-bed reactor top, enter beds after mixing with circulatory mediator, carry out Fischer-Tropsch synthesis, all products flow out from fixed-bed reactor bottom; Or unstripped gas opening for feed from fixed-bed reactor bottom enters, and liquid product flows out from reactor bottom, and gaseous product flows out from top;
(4) reaction product is all collected and is then carried out oil gas water three phase separation, the synthetic water of separating enters wastewater treatment equipment, the gas of separating enters circular buffering tank, after entering stable state, a part is made other purposes as the venting of speeding, and another part and fresh synthesis gas converge as unstripped gas; The liquid of separating enters rectifying tower and carries out further separation, the C that separation is obtained
5-C
8a part as circulatory mediator, use, all the other make other purposes.
As mentioned above, a kind of for without detrimental impurity, that do not participate in reaction, resistant to elevated temperatures porcelain ring, aluminium ball, silicon ball etc. of thinner.
As mentioned above, the catalyzer that Fischer-Tropsch synthesis process adopts comprises can be for all cobalt-base catalysts of Fischer-Tropsch synthesis.
The method preparation that catalyzer can be described by Chinese patent CN102962077A: prepare a certain amount of sodium aluminate aqueous solution, splash into ammoniacal liquor, water-bath keeps for some time, then adds peptizing agent HNO
3, stirring and refluxing is to being transparent colloidal sol, keeps for some time, then the aging gel that makes at room temperature.Gel is put in loft drier dry, then by xerogel in microwave oven Program intensification roasting, make support of the catalyst.By final catalyzer, form the Co (NO of preparation
3)
26H
2o-LaCl
37H
2o-IrCl
33H
2the O aqueous solution, impregnated in above-mentioned carrier, and dry, roasting, makes Co/La/Ir/Al catalyzer, and its weight consists of Co
3o
4: LaO
2: IrO
2: Al
2o
3=100:5-15:2-3:300-500.
Or the method preparation that can describe by patent CN101269328: a certain amount of Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES of 9.06g is dissolved in butanols and is stirred evenly by final catalyzer, add a certain amount of stearylamine, fully dissolve, add again a certain amount of water and butyl (tetra) titanate, stir, decompression rotary evaporation is dry, and roasting, makes Co/TiO
2catalyzer, catalyst weight consists of Co:TiO
2=15-40:100.
Or the method preparation that can describe by patent CN101269336: take porous-starch gel as template, taking a certain amount of potato starch is added to the water, heated and stirred, refrigerating chamber in-20 ℃ after room temperature is standing is placed, and then dry under room temperature, make the porous-starch gel with ordered structure.By final catalyzer, form obtain solution TEOS-EtOH-NH
3-Co-Re the aqueous solution stirs this solution under room temperature, and then three steps are impregnated in the duct of starch template, and dry, under air atmosphere, starch template is removed in roasting, makes Co-Re-SiO
2catalyzer, its catalyst weight consists of Co:Re:SiO
2=100:0.1-1.0:300-600.
As mentioned above, in Fischer-Tropsch building-up process, catalyzer reduces in pure hydrogen atmosphere, and reductive condition is: 350-450 ℃, 0.5-1.0MPa, 500-1500h
-1(v/v), 6-12h; Reaction conditions is: 170-250 ℃, synthesis gas composition is H
2: CO(v/v)=1.5-3:1, synthetic gas dividing potential drop is 2.0-3.0MPa, volume space velocity is 500-2500h
-1(v/v), the volume ratio of circulation gas and fresh synthesis gas is 1-5:1.In view of circulatory mediator partly volatilizees, occupy system dividing potential drop, need suitable raising system stagnation pressure, to guarantee effective dividing potential drop of synthetic gas.
Above method for preparing catalyst is only for explaining the present invention, and do not limit the method for preparing catalyst the present invention relates to.
As mentioned above, circulatory mediator is C
5-C
8liquid state list alkane or C
5-C
8liquid alkane mixture, it derives from, and system is outer adds or the interior product separation of system.
As mentioned above, circulatory mediator can be that reactor is entered in independent preheating, can also with the laggard reactor of unstripped gas mixing preheating.
As mentioned above, circulatory mediator can soak beds in advance, also can be not wetting in advance.
As mentioned above, the weight ratio of circulatory mediator and unstripped gas is 1-20:1, in reaction, initially need to out-of-bounds provide corresponding circulatory mediator.
Technique of the present invention has advantages of that heat exchange efficiency is high, bed temperature evenly, stable operation be easy to control, and there is C
5 +the outstanding advantages that selectivity is high, methane selectively is low and operation air speed is large, product yield is high.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Fig. 2 is embodiment 1 bed temperature scatter chart.
Fig. 3 is embodiment 2 bed temperature scatter charts.
Fig. 4 is embodiment 3 bed temperature scatter charts.
As shown in the figure: 1-spraying gun, 2-reactor, 3-three phases separator, 4-unstripped gas, 5-interchanger, 6-fresh synthesis gas, 7-circulation gas, 8-speeds to exit, 9-circular buffering tank, 10-synthetic water, 11-rectifying tower, 12-liquor pump, 13-C
5-C
8cut, 14-heavy oil, 15-soft wax, 16-hard wax, 17-interchanger, 18-circulatory mediator.
Embodiment
For a better understanding of the present invention, provide below several illustrative but be not restrictive embodiment.
Embodiment 1:
The method Kaolinite Preparation of Catalyst Co/La/Ir/Al describing by Chinese patent CN102962077A: the sodium aluminate aqueous solution of preparing a certain amount of 0.5mol/L, splash into 2ml ammoniacal liquor, keeping temperature is 65 ℃, and hold-time 60min, is then that 0.1:1 adds peptizing agent HNO by sol and sodium aluminate mol ratio
3, stirring and refluxing, to being transparent colloidal sol, keeps 3h, and then under room temperature, aging 12h makes gel.Gel is put in loft drier in 105 ℃ of dry 6h, then xerogel is placed in to temperature programming microwave oven, 2 ℃/min of temperature rise rate, at 350 ℃, roasting 10h, makes support of the catalyst.22 (wt) %, 3 (wt) % and 0.5% that by tricobalt tetroxide, lanthanum trioxide and iridium dioxide, account for respectively final catalyzer take Co (NO
3)
26H
2o, LaCl
37H
2o and IrCl
33H
2o, measures deionized water according to equi-volume impregnating, is mixed with mixing salt solution and impregnated in above-mentioned carrier, and dipping time is 5h, then at 100 ℃, is dried 6h, and finally at 250 ℃ of roasting 15h, 3 ℃/min of temperature rise rate, makes catalyzer, and compressing tablet screening is standby.Final catalyst weight is Co
3o
4: LaO
2: IrO
2: Al
2o
3=22:2.5:0.5:75.
Get this catalyzer of 20-40 object 100ml and be loaded on fixed-bed reactor, internal diameter 14mm, the about 900mm of bed height.On bed 1/3 section with the dilution of porcelain ring/catalyzer (v/v)=1:3, in the middle of bed 1/3 section with porcelain ring/catalyzer (v/v)=1:5 dilution, bed lower 1/3 section with porcelain ring/catalyzer (v/v)=1:10 dilution.Catalyzer reduces in pure hydrogen, and reductive condition is 410 ℃, 0.8MPa, 500h
-1(v/v), 20h.After reduction, cooling switching synthetic gas reacts, and reacts 220 ℃ of temperature synthetic gas dividing potential drop 2.2MPa, H
2: CO(v/v)=1.5:1, feed gas volume air speed 2000h
-1under carry out, the volume ratio of circulation gas and fresh synthesis gas is 1.Fresh synthesis gas 6 (240L/h) is preheated to 180 ℃ through preheater 5, and through preheater 17, is preheated to the C of 170 ℃
5-C
8cut 13 (4.9L/h) enters beds from fixed-bed reactor 2 tops after mixing.All products flow out from reactor bottom, then reaction product is all collected and is carried out separation at three phases separator 3, the synthetic water 10 of separating enters wastewater treatment equipment, the gas of separating enters circular buffering tank 9, after entering stable state, a part (45L/h), as speeding to exit 8, is made other purposes, a part (240L/h) is made circulation gas 7, converges as unstripped gas 4 with fresh synthesis gas (240L/h); The liquid of separating enters rectifying tower 11 and carries out further cutting and separating, the C that separation is obtained
5-C
8a part (4.9L/h) for cut (boiling range is 28 ℃ to 126 ℃) is used as circulatory mediator, and oil gas weight ratio is about 15:1, and all the other make other purposes.Under this operating mode, CO per pass conversion is 81.3%, and methane selectively is 3.23%, C
5 +space-time yield is 0.35g/ml
cath.This operating mode lower bed layer temperature distributing curve diagram is shown in curve a in Fig. 2, curve b is bed temperature distribution curve when oil circulation, correlation curve a, b are visible, when oil circulation, the bed temperature difference can reach 21 ℃, and when oil circulation, the bed temperature difference is only 5.5 ℃, and the very mild homogeneous of whole bed temperature, reactor utilization ratio is high, and throughput is large, and bed is without focus.Final product distributes as shown in table 1.
Table 1 embodiment 1 final product distribution table
Embodiment 2:
The method Kaolinite Preparation of Catalyst Co/TiO describing by patent CN101269328
2, 9.06g Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES is dissolved in 350ml butanols and is stirred evenly, add a certain amount of stearylamine (mol ratio C
18-NH
3/ Co=3), fully dissolve, then add the water of 6.8ml, finally add 24ml butyl (tetra) titanate, continue to adopt decompression rotary evaporation dry after stirring 24h, 100 ℃ dry, and last 500 ℃ of roasting 6h, make catalyzer, and its weight consists of Co:TiO
2=25.5:100, compressing tablet screening is standby.
Get this catalyzer of 20-40 object 100ml and be loaded on fixed-bed reactor, internal diameter 14mm, the about 900mm of bed height.On bed 1/3 section with the dilution of aluminium ball/catalyzer (v/v)=1:2, in the middle of bed 1/3 section with aluminium ball/catalyzer (v/v)=1:9 dilution, lower 1/3 section of bed does not dilute.Catalyzer reduces in pure hydrogen, and reductive condition is 380 ℃, 0.6MPa, 1200h
-1(v/v), 18h.After reduction, cooling switching synthetic gas reacts, and reacts 200 ℃ of temperature synthetic gas dividing potential drop 2.5MPa, H
2: CO(v/v)=2:1, feed gas volume air speed 1000h
-1under carry out, the volume ratio of circulation gas and fresh synthesis gas is 2.Fresh synthesis gas 6 (120L/h) is preheated to 200 ℃ through preheater 4 and enters reactor 2, C from lower opening for feed
5-C
8cut 13 (1.2L/h) enters reactor 2 from upper feeding mouth after preheater 17 is preheated to 170 ℃.All products flow out from reactor bottom, then reaction product is all collected and is carried out separation at three phases separator 3, the synthetic water 10 of separating enters wastewater treatment equipment, the gas of separating enters circular buffering tank 9, after entering stable state, a part (45L/h), as speeding to exit 8, is made other purposes, a part (240L/h) is made circulation 7 gas, converges as unstripped gas 4 with fresh synthesis gas (120L/h); The liquid of separating enters rectifying tower 11 and carries out further cutting and separating, the C that separation is obtained
5-C
8a part (1.2L/h) for cut (boiling range is 28 ℃ to 126 ℃) is used as circulatory mediator, and oil gas weight ratio is about 5:1, and all the other make other purposes.Under this operating mode, CO per pass conversion is 70.8%, and methane selectively is 4.73%, C
5 +space-time yield is 0.15g/ml
cath.This operating mode lower bed layer temperature distributing curve diagram is shown in curve a in Fig. 3, and curve b is bed temperature distribution curve when oil circulation.Correlation curve a, b are visible, and the bed temperature difference can reach 14.5 ℃ when oil circulation, and bed focus is fairly obvious, and temperature runaway very easily has bed temperature difference when oil circulation to be only 5.5 ℃, and bed, without obvious focus, is not easy temperature runaway, and whole bed utilization ratio is high, and reactor efficiency is high.Final product distributes as shown in table 2.
Table 2 embodiment 2 final product distribution tables
Embodiment 3:
Press the method Kaolinite Preparation of Catalyst Co/Re/Si that Chinese patent CN101269336 describes, take porous-starch gel as template, taking 10g potato starch joins in 100g water, be heated to 90 ℃ and stir after the standing 12h of 10min. room temperature, in the porous-starch gel that the refrigerating chambers of-20 ℃ are placed 12h and then dry 24h must have ordered structure under room temperature.Obtain solution TEOS:EtOH:NH
3: H
2o:Co:Re=1:30:0.15:0.45:0.02 stirs 8h by this solution under room temperature, and then three steps are impregnated in the duct of starch template (starch gel/starch gel+solution=20 (wt%)).Every step dipping 12 hours, 120 ℃ of dry 24h.Finally under 550 ℃ of air atmospheres, roasting is removed starch template in 8 hours, and making containing Co is that 7.5wt%, Re are 2wt%, SiO
2for the catalyzer of 70.5wt%, compressing tablet screening is standby.
Get this catalyzer of 20-40 object 100ml and be loaded on fixed-bed reactor, internal diameter 14mm, the about 900mm of bed height.On bed 1/3 section with the dilution of silicon ball/catalyzer (v/v)=1:5, in the middle of bed 1/3 section with silicon ball/catalyzer (v/v)=1:4 dilution, bed lower 1/3 section with silicon ball/catalyzer (v/v)=1:5 dilution.Catalyzer reduces in pure hydrogen, and reductive condition is 350 ℃, 0.7MPa, 1500h
-1(v/v), 10h.After reduction, cooling switching synthetic gas reacts, and reacts 210 ℃ of temperature synthetic gas dividing potential drop 2.0MPa, H
2: CO(v/v)=2.5:1, unstripped gas air speed 2000h
-1under carry out, the volume ratio of circulation gas and fresh synthesis gas is 3.Fresh synthesis gas 6 (240L/h) is preheated to 180 ℃ through preheater 4, and through preheater 17, is preheated to the C of 170 ℃
5-C
8cut 13 (6.5L/h) enters beds from fixed-bed reactor 2 tops after mixing.All products flow out from reactor bottom, then reaction product is all collected and is carried out separation at three phases separator 3, the gas of separating enters circular buffering tank 9, after entering stable state, a part (88L/h) is as speeding to exit 8, make other purposes, a part (720L/h) is made circulation gas 7, converges as unstripped gas 4 with fresh synthesis gas (240L/h); The liquid of separating enters rectifying tower 11 and carries out further cutting and separating, the C that separation is obtained
5-C
8a part (6.5L/h) for cut (boiling range is 28 ℃ to 126 ℃) is used as circulatory mediator, and oil gas weight ratio is about 10:1, and all the other make other purposes.Under this operating mode, CO per pass conversion is 63.3%, and methane selectively is 5.75%, C
5 +space-time yield is 0.27g/ml
cath.This operating mode lower bed layer temperature distributing curve diagram is shown in curve a in Fig. 4, and curve b is bed temperature distribution curve when oil circulation.Correlation curve a, b are visible, and the bed temperature difference can reach 14 ℃ when oil circulation, and when oil circulation, the bed temperature difference is only 7 ℃, bed temperature fluctuation when oil circulation, amplitude is very large, has when oil circulation and bed temperature only has fuctuation within a narrow range, bed temperature is milder, and bed is without obvious focus.Final product distributes as shown in table 3.
Table 3 embodiment 3 final product distribution tables
Claims (9)
1. be applicable to a Fischer-Tropsch synthesis process for fixed-bed reactor, it is characterized in that comprising the steps:
(1) bed is divided into upper, middle and lower segment, the catalyzer that need to load three bed sections, fills out than for 0-1:1 dilutes laggard luggage by thinner and catalyst volume;
(2) circulatory mediator is preheated to after the temperature of supercritical state under reaction pressure, from the top of fixed-bed reactor, enters beds;
(3) fresh synthesis gas and circulation gas enter beds from fixed-bed reactor upper feeding mouth separately after being mixed to form unstripped gas preheating, or from fixed-bed reactor top, enter beds after mixing with circulatory mediator, carry out Fischer-Tropsch synthesis, all products flow out from fixed-bed reactor bottom; Or unstripped gas opening for feed from fixed-bed reactor bottom enters, and liquid product flows out from reactor bottom, and gaseous product flows out from top;
(4) reaction product is all collected and is then carried out oil gas water three phase separation, the synthetic water of separating enters wastewater treatment equipment, the gas of separating enters circular buffering tank, after entering stable state, a part is made other purposes as the venting of speeding, and another part and fresh synthesis gas converge as unstripped gas; The liquid of separating enters rectifying tower and carries out further separation, the C that separation is obtained
5-C
8a part as circulatory mediator, use, all the other make other purposes.
2. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, is characterized in that described thinner is a kind of in porcelain ring, aluminium ball, silicon ball.
3. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, it is characterized in that catalyzer that described Fischer-Tropsch synthesis adopts comprises can be for all cobalt-base catalyst of Fischer-Tropsch synthesis.
4. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 3, is characterized in that described cobalt-base catalyst is Co/La/Ir/Al catalyzer, and its weight consists of Co
3o
4: LaO
2: IrO
2: Al
2o
3=100:5-15:2-3:300-500; Co/TiO
2catalyzer, its weight consists of Co:TiO
2=15-40:100; Or Co-Re-SiO
2catalyzer, its catalyst weight consists of Co:Re:SiO
2=100:0.1-1.0:300-600.
5. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, it is characterized in that in described Fischer-Tropsch building-up process, catalyzer reduces in pure hydrogen atmosphere, reductive condition is: 350-450 ℃, 0.5-1.0MPa, volume space velocity 500-1500h
-1, 6-12h; Reaction conditions is: 170-250 ℃, synthesis gas composition is H
2: CO volume ratio=1.5-3:1, synthetic gas dividing potential drop is 2.0-3.0MPa, volume space velocity is 500-2500h
-1, the volume ratio of circulation gas and fresh synthesis gas is 1-5:1.
6. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, is characterized in that described circulatory mediator is C
5-C
8liquid state list alkane or C
5-C
8liquid alkane mixture, it derives from, and system is outer adds or the interior product separation of system.
7. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, it is characterized in that described circulatory mediator also with the laggard reactor of unstripped gas mixing preheating.
8. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, is characterized in that described circulatory mediator wetting beds in advance, or not wetting in advance.
9. a kind of Fischer-Tropsch synthesis process that is applicable to fixed-bed reactor as claimed in claim 1, is characterized in that described circulatory mediator and the weight ratio of unstripped gas are 1-20:1.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106391019A (en) * | 2015-07-31 | 2017-02-15 | Ifp 新能源公司 | Process for the preparation of a catalyst intended for use in a fischer-tropsch reaction |
| CN105087042B (en) * | 2014-05-09 | 2018-04-13 | 中国石油化工股份有限公司 | A kind of method of F- T synthesis |
| CN110201609A (en) * | 2019-06-13 | 2019-09-06 | 江南大学 | A kind of device and method adding hydrogen coproduction alkene and aromatic hydrocarbons using synthesis gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102211002A (en) * | 2010-04-12 | 2011-10-12 | 中科合成油技术有限公司 | Hot oil circulating and cold quenching fixed bed Fischer-Tropsch synthesis reactor and application thereof |
| US20120129961A1 (en) * | 2009-06-10 | 2012-05-24 | IFP Energies Nouvelles | Method for optimizing the operation of a hydrocarbon synthesis unit starting from synthesis gas, by controlling the partial pressure of co |
-
2013
- 2013-12-09 CN CN201310659132.0A patent/CN103695022B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120129961A1 (en) * | 2009-06-10 | 2012-05-24 | IFP Energies Nouvelles | Method for optimizing the operation of a hydrocarbon synthesis unit starting from synthesis gas, by controlling the partial pressure of co |
| CN102211002A (en) * | 2010-04-12 | 2011-10-12 | 中科合成油技术有限公司 | Hot oil circulating and cold quenching fixed bed Fischer-Tropsch synthesis reactor and application thereof |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105087042B (en) * | 2014-05-09 | 2018-04-13 | 中国石油化工股份有限公司 | A kind of method of F- T synthesis |
| CN106391019A (en) * | 2015-07-31 | 2017-02-15 | Ifp 新能源公司 | Process for the preparation of a catalyst intended for use in a fischer-tropsch reaction |
| CN106391019B (en) * | 2015-07-31 | 2021-05-11 | Ifp 新能源公司 | Process for preparing a catalyst intended to be used in the fischer-tropsch reaction |
| CN110201609A (en) * | 2019-06-13 | 2019-09-06 | 江南大学 | A kind of device and method adding hydrogen coproduction alkene and aromatic hydrocarbons using synthesis gas |
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