CN204710288U - A kind of fischer-tropsch catalysts reduction reactor - Google Patents
A kind of fischer-tropsch catalysts reduction reactor Download PDFInfo
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- CN204710288U CN204710288U CN201520412326.5U CN201520412326U CN204710288U CN 204710288 U CN204710288 U CN 204710288U CN 201520412326 U CN201520412326 U CN 201520412326U CN 204710288 U CN204710288 U CN 204710288U
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- 239000003054 catalyst Substances 0.000 title claims abstract description 111
- 230000009467 reduction Effects 0.000 title claims abstract description 104
- 239000000428 dust Substances 0.000 claims abstract description 17
- 239000007787 solid Substances 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 239000002245 particle Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 abstract description 25
- 238000003786 synthesis reaction Methods 0.000 abstract description 25
- 239000000843 powder Substances 0.000 abstract description 23
- 239000000203 mixture Substances 0.000 abstract description 8
- 230000003213 activating effect Effects 0.000 abstract description 4
- 230000003993 interaction Effects 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 71
- 239000007789 gas Substances 0.000 description 45
- 238000000034 method Methods 0.000 description 18
- 238000001994 activation Methods 0.000 description 17
- 230000004913 activation Effects 0.000 description 14
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 10
- 238000009826 distribution Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- 238000011946 reduction process Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000008520 organization Effects 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 230000037452 priming Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229910000859 α-Fe Inorganic materials 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000006188 syrup Substances 0.000 description 1
- 235000020357 syrup Nutrition 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of fischer-tropsch catalysts reduction reactor, it is characterized in that, described reduction reactor comprises columnar reduction section, be connected with the upper end of described reduction section one and the undergauge section coaxial with described reduction section and the dust separation section that is integrally made up of changeover portion and the diameter extension diameter section larger than described reduction section, and the lower end of described changeover portion and the lower end outer surface of described undergauge section are tightly connected the cavity making described undergauge section be positioned at described dust separation section.The outlet of undergauge section is provided with fast gas-solid separator, and the fine powder in gas is separated rapidly after interaction with the target molecules and falls into bottom dust separation section and to discharge reduction reactor system.Adopt fischer-tropsch catalysts reduction reactor of the present utility model to carry out catalyst reduction, the fast restore of catalyst can be realized, and the granularmetric composition of activating catalyst can be controlled, improve the job stability of synthesis reactor.
Description
Technical field
The utility model relates to a kind of fischer-tropsch catalysts reduction reactor.
Background technology
For improving the reactivity worth of fischer-tropsch catalysts, must activate before use, developing various activating apparatus and method according to the characteristic of fischer-tropsch catalysts and technological requirement at present.For the precipitated iron-based catalyst that Low Temperature Fischer Tropsch synthesis technique is conventional, general employing slurry bed system activating process.Adopt H
2, CO or synthesis gas carry out pretreatment (activation) to catalyst, preprocessing process comprises two processes: first will containing Fe
2o
3catalyst fast transition be Fe
3o
4, then by Fe
3o
4experience a conversion process slowly, become α-Fe and Fe
3o
4mixture (use H
2reduction) or χ-Fe
5c
2(using CO or synthesis gas reduction).Research finds: the active component after fischer-tropsch catalysts activation is α-Fe, χ-Fe
5c
2or the mixture of the two, the ratio of the two is relevant with the activation condition such as activation phenomenon, soak time.
Publication number is the Chinese patent application of CN1562484A, discloses a kind of method of reducing of syrup state bed Fischer Tropsch synthesis iron base catalyst.Although catalyst reduction can be available fischer-tropsch reaction catalyst by slurry bed system reduction apparatus and technique, but the catalyst fines having that reduction apparatus is bulky, the recovery time is long, catalyst abrasion is serious, produce in reduction process cannot be separated, activity is difficult to keep and the series of problems such as organization of production difficulty after catalyst replacement, makes to fail to realize plant-scale application always.In addition, the molecule produced in catalyst activation process, after entering Fischer-Tropsch synthesis device, by the filter of Severe blockage reactor, increases filtration pressure drop and the blowback frequency of filter, is unfavorable for the normal tissue produced.
Publication number is the industrial reduction method that the Chinese patent application of CN1814350A discloses a kind of particle iron-base fischer-tropsch synthesis catalyst, and the method is a catalyst reduction process independent of Fischer-Tropsch synthesis.Reduction process is carried out in independently reduction reactor, and be divided into reduction phase and adjusting stage, operating temperature is 260-450 DEG C, and pressure is 1.5-5.0MPa, and inlet velocity is 0.15-0.7m/s, and fluid bed emulsion zone caltalyst volume concentrations is 5-60%.Reducing gas adopts H
2or CO, or H
2with the gaseous mixture of CO.Reducing process flow process comprises following equipment: compressor, heating heat exchanger, cooling heat exchanger, reduction reactor, dust arrester, vapour liquid separator, catalyst reduction raw material tank and catalyst charge groove.The gas access linear speed of this catalyst reduction method is 0.15-0.7m/s, the excessive wear that the fluid bed reduction reactor operating in this high linear speed will cause catalyst in reduction process, there is a large amount of superfines after reduction in product.When reducing catalyst enters participation reaction in slurry bed system synthesis reactor, also will greatly increase the filter pressure of fischer-tropsch synthesis process middle filtrator, increase filter recoil number of times, increase operating cost and also shorten its service life.Further, the recovery time of the method is longer, is generally 36-72 hour; Reduction reactor operating pressure is higher, is 1.5-5.0MPa, belongs to high temperature and high pressure containers, manufactures, operation and maintenance cost is higher.
Utility model content
The purpose of this utility model is to provide a kind of fischer-tropsch catalysts reduction reactor, this reduction reactor is used to reduce to fischer-tropsch catalysts, the fast restore of catalyst can be realized, and the granularmetric composition of activating catalyst can be controlled, improve the job stability of synthesis reactor.
To achieve these goals, the utility model provides a kind of fischer-tropsch catalysts reduction reactor, it is characterized in that, described reduction reactor comprises columnar reduction section 1, be connected with the upper end of described reduction section 1 one and the undergauge section 2 coaxial with described reduction section 1 and the dust separation section that is integrally made up of changeover portion 3 and the diameter extension diameter section 4 larger than described reduction section 1, and the lower end of described changeover portion 3 and the lower end outer surface of described undergauge section 2 are tightly connected the cavity making described undergauge section 2 be positioned at described dust separation section; Described reduction section 1 top is provided with the catalyst inlet 5 for sending into catalyst to be restored, and the bottom of reduction section 1 is provided with reducing gas entrance 6, and the bottom of reduction section 1 is provided with reducing catalyst outlet 7; The top of described undergauge section 2 is positioned at the gas-solid quick disconnector 9 above described undergauge section gas vent 8 with being provided with undergauge section gas vent 8 for sending catalyst fines and reduction tail gas and relative spacing; The bottom of described changeover portion 3 is provided with catalyst fines outlet 10; The top sealing plate of described extension diameter section 4 is provided with the offgas outlet 11 for sending reduction tail gas.
Preferably, described reduction reactor is gas-particle two-phase fluidized-bed reactor or internal recycling zero gradient reactor, is preferably fixed fluidized-bed reactor.
Preferably, the ratio of height to diameter of described reduction section 1 is 3-10, and the ratio of height to diameter of described extension diameter section 4 is 2-6.
Preferably, the diameter of described extension diameter section 4 and the diameter ratio of described reduction section 1 are 1.5-5.0, are preferably 2-3; The upper port diameter of described undergauge section 2 and the diameter ratio of described reduction section 1 are 0.7-1.0, are preferably 0.85-0.95.
Preferably, the bottom in described reduction section 1 cavity is provided with the gas distributor 13 for the reducing gas sending into described reduction section 1 that distributes.
Preferably, described gas distributor 13 is for being selected from least one form in single flow, lateral flow type, tubular type, bubble cap formula and wire netting.
Preferably, described gas-solid quick disconnector 9 is umbrella hat type, ejection type, side channel formula or T-shaped elbow type gas-solid quick disconnector, preferred umbrella hat type gas-solid quick disconnector.
Preferably, the angle between the periphery wall of described changeover portion 3 and horizontal plane is greater than the angle of repose of the catalyst fines deposited in described extension diameter section.
Preferably, it is characterized in that, described offgas outlet 11 is by the cavity fluid UNICOM of dust filter unit 12 with described extension diameter section 4.
The fischer-tropsch catalysts reduction reactor that the utility model provides, tool has the following advantages:
1, the gas-liquid-solid phase reaction in slurry bed system activated reactor is converted to gas-particle two-phase reaction, improves mass transfer rate and the reaction rate of catalyst reduction reaction, reduce reactor scale, improve the production capacity of device;
2, by the design of activated reactor, the fine powder produced in catalyst reduction process is separated with large granular catalyst, fine powder content in reducing catalyst product is reduced, alleviates the filter pressure of Fischer-Tropsch synthesis device;
3, reducing catalyst can directly be stored in the closed container protected by synthesis gas, convenient transport and using, can quick-replaceable when in synthesis reactor, catalyst needs to change, and organization of production is convenient.
Other feature and advantage of the present utility model are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for description, is used from explanation the utility model, but does not form restriction of the present utility model with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the schematic diagram of a kind of detailed description of the invention of the fischer-tropsch catalysts reduction reactor that the utility model provides.
Description of reference numerals
1 reduction section 2 undergauge section 3 changeover portion 4 extension diameter section 5 catalyst inlet
6 reducing gas entrance 7 reducing catalysts export 8 undergauge section gas vents
9 gas-solid quick disconnector 10 catalyst fines export 11 offgas outlet 12 dust filter units
13 gas distributor 14 catalyst emission pipeline 15 fine powder discharge pipes
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of fischer-tropsch catalysts reduction reactor, it is characterized in that, described reduction reactor comprises columnar reduction section 1, be connected with the upper end of described reduction section 1 one and the undergauge section 2 coaxial with described reduction section 1 and the dust separation section that is integrally made up of changeover portion 3 and the diameter extension diameter section 4 larger than described reduction section 1, and the lower end of described changeover portion 3 and the lower end outer surface of described undergauge section 2 are tightly connected the cavity making described undergauge section 2 be positioned at described dust separation section; Described reduction section 1 top is provided with the catalyst inlet 5 for sending into catalyst to be restored, and the bottom of reduction section 1 is provided with reducing gas entrance 6, and the bottom of reduction section 1 is provided with reducing catalyst outlet 7; The top of described undergauge section 2 is positioned at the gas-solid quick disconnector 9 above described undergauge section gas vent 8 with being provided with undergauge section gas vent 8 for sending catalyst fines and reduction tail gas and relative spacing; The bottom of described changeover portion 3 is provided with catalyst fines outlet 10; The top sealing plate of described extension diameter section 4 is provided with the offgas outlet 11 for sending reduction tail gas.
According to the utility model, described fischer-tropsch catalysts is well-known to those skilled in the art, can be graininess, microspheroidal or powdery, is preferably metallic catalyst, is more preferably iron-base fischer-tropsch synthesis catalyst.
According to the utility model, described reduction reactor refers to for reducing the reactor of fischer-tropsch catalysts, can be Dual-Phrase Distribution of Gas olid fluidized bed reactor or internal recycling zero gradient reactor, be preferably fixed fluidized-bed reactor.
According to the utility model, the ratio of height to diameter of described reduction section 1 can be 3-10, is preferably 4-8, is more preferably 5-6; The ratio of height to diameter of described extension diameter section 4 can be 2-6, is preferably 3-4; The diameter of described extension diameter section 4 and the diameter ratio of described reduction section 1 can be 1.5-5.0, are preferably 2-3; The upper port diameter of described undergauge section 2 and the diameter ratio of described reduction section 1 can be 0.7-1.0, are preferably 0.85-0.95.
According to the utility model, the fine powder that gas-solid quick disconnector 9 is carried secretly to be separated described reduction tail gas with particles settling can be utilized in described dust separation section, and fine powder discharges reduction reactor by the bottom of described dust separation section, the particle size range isolating fine powder can for being less than 60 μm, preferably be less than 50 μm, be more preferably less than 30 microns.Described gas-solid quick disconnector is well-known to those skilled in the art, such as, can be umbrella hat type, ejection type, side channel formula or T-shaped elbow type gas-solid quick disconnector, is preferably umbrella hat type gas-solid quick disconnector.Wherein, the gas-solid quick disconnector of described umbrella hat type and the beeline of described undergauge section gas vent 8 can be 1-2 times of described undergauge section 2 diameter.
According to the utility model, angle between the perisporium of described changeover portion 3 and horizontal plane is not less than the angle of repose of the catalyst fines deposited in described extension diameter section, described angle of repose is well-known to those skilled in the art, refer in gravitational field, when particle slides on the free inclined-plane of powder accumulation horizon, between suffered gravity and particle, frictional force reaches balance and the maximum angular that records under remaining static.
According to the utility model, the bottom in described reduction section 1 cavity can be provided with the gas distributor 13 for the reducing gas sending into described reduction section 1 that distributes; The height of described gas distributor 13 can lower than described reducing catalyst outlet 7.Wherein, described gas distributor is well-known to those skilled in the art, for being selected from least one form in single flow, lateral flow type, tubular type, bubble cap formula and wire netting, can being preferably tubular type and/or emitting bubble, being more preferably tubular type.
According to the utility model, described offgas outlet 11 can by the cavity fluid UNICOM of dust filter unit 12 with described extension diameter section 4.Described dust filter unit is well-known to those skilled in the art, may be used for the catalyst fines filtering non-sedimentation in reduction tail gas, described pneumatic filter preferably uses the filter of high efficiency low pressure drop, to reduce the overall pressure drop of reduction reactor system, reduces power consumption.
According to the utility model, described reducing catalyst outlet 7 can be communicated with reducing catalyst after-treatment system by catalyst emission pipeline 14; The inclination angle of described catalyst emission pipeline 14 is not less than the angle of repose of reducing catalyst.Described fine powder outlet 10 can be communicated with catalyst fines treatment system by fine powder discharge pipe 15; The inclination angle of described fine powder discharge pipe 15 is not less than the angle of repose of catalyst fines.
To further illustrate the utility model by embodiment below, but therefore the utility model is not subject to any restriction.The catalyst grain size distribution of the utility model embodiment adopts GB/T19077.1-2003 method to measure.
Embodiment 1:
As shown in Figure 1: in the activated reactor that expanding ratio is 2, add catalyst 1kg to be restored, at normal temperatures and pressures that the air displacement in activation system is complete with nitrogen, with H
2: the reducing gas composition of CO=20:1 passes into reducing gases to restoring system, makes the pressure of priming reaction system be elevated to 0.1MPa, maintains gas empty tower gas velocity 0.06m/s constant during boosting.Then according to reduction activation heating curve by reactor heat temperature raising, at 260 DEG C, carry out constant temperature reductase 12 0h to catalyst, dense fluidized district caltalyst volume concentrations is between 65-70%.After reduction terminates, keep activation system reducing gas air speed constant with reduction pressure, stop reactor heating, temperature of reactor to be restored is down to 50 DEG C, is entered by catalyst in the closed container under synthesis gas protection, becomes product for synthesis technique.
Weigh the weight of catalyst bulky grain and fine powder respectively, bulky grain accounting is 96.44%, and fine powder accounting is 1.80%, loss 1.76%.The granularmetric composition of application laser particle analyzer to untreated catalyst, catalyst bulky grain, catalyst fines is analyzed, in table 1.
As shown in table 1, catalyst is after reduction activation, and the radial small-particle direction of catalyst pellets is moved, and has occurred the fine powder of some; Described reduction activation device can remove the fine powder produced in catalyst activation process preferably, keep the oarse-grained size distribution of catalyst and untreated catalyst basically identical.By regulating reducing gas empty tower gas velocity, can make further the oarse-grained size distribution of catalyst and untreated catalyst completely the same.Namely the fine powder produced in fine powder in catalyst raw material and reduction process can be removed in the lump, make the catalyst entering synthesis reactor be bulky grain, reduce the filter pressure of synthesis reactor, improve the parallel-adder settle-out time of synthesis reactor.
The size distribution of table 1 catalyst
Embodiment 2:
As shown in Figure 1: in the activated reactor that expanding ratio is 2, add catalyst 1kg to be restored, at normal temperatures and pressures that the air displacement in activation system is complete with nitrogen, with H
2: the reducing gas composition of CO=5:1 passes into reducing gases to restoring system, makes the pressure of priming reaction system be elevated to 0.2MPa, maintains gas empty tower gas velocity 0.2m/s constant during boosting.Then according to reduction activation heating curve by reactor heat temperature raising, at 300 DEG C to catalyst carry out constant temperature reduction 12h, dense fluidized district caltalyst volume concentrations is between 55-60%.After reduction terminates, keep activation system reducing gas air speed constant with reduction pressure, stop reactor heating, temperature of reactor to be restored is down to 80 DEG C, is entered by catalyst in the closed container under synthesis gas protection, becomes product for synthesis technique.
Weigh the weight of catalyst bulky grain and fine powder respectively, bulky grain accounting is 97.97%, and fine powder accounting is 0.91%, loss 1.12%.The granularmetric composition of application laser particle analyzer to untreated catalyst, catalyst bulky grain, catalyst fines is analyzed, in table 2.
As shown in table 2, catalyst is after reduction activation, and the radial small-particle direction of catalyst pellets is moved, and has occurred the fine powder of some; Described reduction activation device can remove the fine powder produced in catalyst activation process preferably, keep the oarse-grained size distribution of catalyst and untreated catalyst basically identical.By regulating reducing gas empty tower gas velocity, can make further the oarse-grained size distribution of catalyst and untreated catalyst completely the same.Namely the fine powder produced in fine powder in catalyst raw material and reduction process can be removed in the lump, make the catalyst entering synthesis reactor be bulky grain, reduce the filter pressure of synthesis reactor, improve the parallel-adder settle-out time of synthesis reactor.
The size distribution of table 2 catalyst
Claims (9)
1. a fischer-tropsch catalysts reduction reactor, is characterized in that,
Described reduction reactor comprises columnar reduction section (1), is connected with the upper end of described reduction section (1) one and the undergauge section (2) coaxial with described reduction section (1) and the dust separation section that is integrally made up of changeover portion (3) and the diameter extension diameter section (4) larger than described reduction section (1), and the lower end of described changeover portion (3) and the lower end outer surface of described undergauge section (2) are tightly connected and make described undergauge section (2) be positioned at the cavity of described dust separation section;
Described reduction section (1) top is provided with the catalyst inlet (5) for sending into catalyst to be restored, the bottom of reduction section (1) is provided with reducing gas entrance (6), and the bottom of reduction section (1) is provided with reducing catalyst outlet (7); The top of described undergauge section (2) is provided with the gas-solid quick disconnector (9) that undergauge section gas vent (8) for sending catalyst fines and reduction tail gas and relative spacing ground are positioned at described undergauge section gas vent (8) top;
The bottom of described changeover portion (3) is provided with catalyst fines outlet (10);
The top sealing plate of described extension diameter section (4) is provided with the offgas outlet (11) for sending reduction tail gas.
2. reduction reactor according to claim 1, is characterized in that, described reduction reactor is gas-particle two-phase fluidized-bed reactor or internal recycling zero gradient reactor, is preferably fixed fluidized-bed reactor.
3. reduction reactor according to claim 1, is characterized in that, the ratio of height to diameter of described reduction section (1) is 3-10, and the ratio of height to diameter of described extension diameter section (4) is 2-6.
4. reduction reactor according to claim 1, is characterized in that, the diameter of described extension diameter section (4) and the diameter ratio of described reduction section (1) are 1.5-5.0, is preferably 2-3; The upper port diameter of described undergauge section (2) and the diameter ratio of described reduction section (1) are 0.7-1.0, are preferably 0.85-0.95.
5. reduction reactor according to claim 1, is characterized in that, the bottom in described reduction section (1) cavity is provided with the gas distributor (13) for the reducing gas sending into described reduction section (1) that distributes.
6. reduction reactor according to claim 5, is characterized in that, described gas distributor (13) is for being selected from least one form in single flow, lateral flow type, tubular type, bubble cap formula and wire netting.
7. reduction reactor according to claim 1, is characterized in that, described gas-solid quick disconnector (9) is umbrella hat type, ejection type, side channel formula or T-shaped elbow type gas-solid quick disconnector, preferred umbrella hat type gas-solid quick disconnector.
8. reduction reactor according to claim 1, is characterized in that, the angle between the periphery wall of described changeover portion (3) and horizontal plane is greater than the angle of repose of the catalyst fines deposited in described extension diameter section (4).
9. reduction reactor according to claim 1, is characterized in that, described offgas outlet (11) is by the cavity fluid UNICOM of dust filter unit (12) with described extension diameter section (4).
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| CN201520412326.5U CN204710288U (en) | 2015-06-15 | 2015-06-15 | A kind of fischer-tropsch catalysts reduction reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106311094A (en) * | 2015-06-15 | 2017-01-11 | 神华集团有限责任公司 | Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method |
| CN106669857A (en) * | 2015-11-10 | 2017-05-17 | 神华集团有限责任公司 | Method for activating precipitated iron Fischer-Tropsch catalyst and Fischer-Tropsch synthesis method |
-
2015
- 2015-06-15 CN CN201520412326.5U patent/CN204710288U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106311094A (en) * | 2015-06-15 | 2017-01-11 | 神华集团有限责任公司 | Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method |
| CN106311094B (en) * | 2015-06-15 | 2024-05-14 | 国家能源投资集团有限责任公司 | Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method |
| CN106669857A (en) * | 2015-11-10 | 2017-05-17 | 神华集团有限责任公司 | Method for activating precipitated iron Fischer-Tropsch catalyst and Fischer-Tropsch synthesis method |
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Address after: No. 22, diazepam West Binhe Road, Dongcheng District, Beijing, Beijing Co-patentee after: NATIONAL INSTITUTE OF CLEAN-AND-LOW-CARBON ENERGY Patentee after: CHINA ENERGY INVESTMENT Corp.,Ltd. Address before: 100011 Shenhua building, 22, Ping Men Road, West Binhe Road, Dongcheng District, Beijing Co-patentee before: NATIONAL INSTITUTE OF CLEAN-AND-LOW-CARBON ENERGY Patentee before: SHENHUA GROUP Corp.,Ltd. |
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Address after: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Patentee after: CHINA ENERGY INVESTMENT Corp.,Ltd. Patentee after: Beijing low carbon clean energy research institute Address before: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Patentee before: CHINA ENERGY INVESTMENT Corp.,Ltd. Patentee before: Beijing low carbon clean energy research institute |