CN106311094A - Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method - Google Patents
Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method Download PDFInfo
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- 239000003054 catalyst Substances 0.000 title claims abstract description 139
- 238000000034 method Methods 0.000 title claims abstract description 42
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- 238000003786 synthesis reaction Methods 0.000 claims abstract description 27
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- 239000007789 gas Substances 0.000 claims description 65
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- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 230000008021 deposition Effects 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 3
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- 238000009826 distribution Methods 0.000 description 8
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- 238000011946 reduction process Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
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- 239000012071 phase Substances 0.000 description 4
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- 229910000859 α-Fe Inorganic materials 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
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- 239000007809 chemical reaction catalyst Substances 0.000 description 1
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Abstract
The invention discloses a Fischer-Tropsch catalyst reduction reactor. The reactor is characterized by including a reduction section, a diameter shrinkage section, and a dust separation section composed of a transition section and a diameter expansion section. The invention also discloses a Fischer-Tropsch catalyst reduction method. According to the method, a to-be-reduced Fischer-Tropsch catalyst is sent into the reduction reactor to conduct reduction treatment under a reducing condition, at the same time the catalyst fine powder in the reduction reactor is separated from a reduced Fischer-Tropsch catalyst product by means of the dust separation section. Use of the Fischer-Tropsch catalyst reduction reactor and reduction method in catalyst reduction can realize rapid reduction of the catalyst, also the grain composition of an activated catalyst can be controlled, and the working stability of a synthesis reactor can be improved.
Description
Technical field
The present invention relates to a kind of fischer-tropsch catalysts reduction reactor and fischer-tropsch catalysts method of reducing.
Background technology
For improving the reactivity worth of fischer-tropsch catalysts, must activate before use, at present according to Fischer-Tropsch
The characteristic of catalyst and technological requirement develop various activation apparatus and method.Work is synthesized for Low Temperature Fischer Tropsch
The precipitated iron-based catalyst that skill is conventional, general employing slurry bed system activating process.Use H2, CO or synthesis
Gas carries out pretreatment (activation) to catalyst, and preprocessing process includes two processes: first will contain Fe2O3
Catalyst fast transition be Fe3O4, then by Fe3O4Experience a conversion process slowly, become
α-Fe and Fe3O4Mixture (use H2Reduction) or χ-Fe5C2(using CO or synthesis gas reduction).
Research finds: the active component after fischer-tropsch catalysts activation is α-Fe, χ-Fe5C2Or the mixture of the two,
The ratio of the two is relevant with the activation condition such as activation phenomenon, soak time.
The Chinese patent application of Publication No. CN1562484A, discloses a kind of syrup state bed Fischer Tropsch synthesis ferrum
The method of reducing of base catalyst.Although catalyst reduction can be available by slurry bed system reduction apparatus and technique
Fischer-tropsch reaction catalyst, but have that reduction apparatus is bulky, recovery time length, catalyst abrasion are tight
Weight, the catalyst fines produced in reduction process cannot separate, after catalyst replacement activity be difficult to keep and
The series of problems such as organization of production difficulty so that always fail to realize plant-scale application.Additionally, urge
Severe blockage, after entering Fischer-Tropsch synthesis device, is reacted by the molecule produced in agent activation process
The filter of device, increases filtration pressure drop and the blowback frequency of filter, is unfavorable for the tissue normally produced.
The Chinese patent application of Publication No. CN1814350A discloses a kind of particle iron-base fischer-tropsch and closes
Becoming the industrial reduction method of catalyst, the method is a catalyst reduction independent of Fischer-Tropsch synthesis
Process.Reduction process is carried out in independent reduction reactor, is divided into reduction phase and metamorphosis stage, behaviour
Being 260-450 DEG C as temperature, pressure is 1.5-5.0MPa, and inlet velocity is 0.15-0.7m/s, fluid bed
Emulsion zone caltalyst volume concentrations is 5-60%.Reducing gas uses H2Or CO, or H2With CO
Gaseous mixture.Reducing process flow process includes 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, and the reduction operating in this high linear speed is anti-
Answer device to will result in catalyst excessive wear in reduction process, product exists after reduction a large amount of micropowder
End.When participating in reaction in reducing catalyst enters slurry bed system synthesis reactor, also will be greatly increased Fischer-Tropsch
The filter pressure of filter in synthesis technique, increases filter recoil number of times, increases operating cost and shorten
Its service life.Further, the recovery time of the method is longer, generally 36-72 hour；Reduction reaction
Device operating pressure is higher, for 1.5-5.0MPa, belongs to high temperature and high pressure containers, manufactures, runs and safeguards into
This is higher.
Summary of the invention
It is an object of the invention to provide a kind of fischer-tropsch catalysts reduction reactor and fischer-tropsch catalysts reduction side
Method, uses this reduction reactor and method of reducing to reduce fischer-tropsch catalysts, can realize catalyst
Fast restore, and the granularmetric composition of activated catalyst can be controlled, improve the working stability of synthesis reactor
Property.
To achieve these goals, first aspect present invention: a kind of fischer-tropsch catalysts reduction reactor is provided,
It is characterized in that, described reduction reactor includes the upper of columnar reduction section 1 and described reduction section 1
Hold one connection and the undergauge section 2 coaxial with described reduction section 1 and compared institute by changeover portion 3 and diameter
State the dust separation section that the big extension diameter section of reduction section 14 is integrally formed, the lower end of described changeover portion 3 and institute
The lower end outer surface stating undergauge section 2 is tightly connected so that described undergauge section 2 is positioned at described dust separation section
In cavity；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 for sending catalyst fines and the undergauge of reduction tail gas
The gas-solid that section gas outlet 8 and relative spacing ground are positioned at above described undergauge section gas outlet 8 quickly divides
From device 9；The bottom of described changeover portion 3 is provided with catalyst fines outlet 10；The top of described extension diameter section 4
The offgas outlet 11 for sending reduction tail gas it is provided with on portion's sealing plate.
Preferably, described reduction reactor is that gas-particle two-phase fluidized-bed reactor or interior circulation are reacted without gradient
Device, 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 is 1.5-5.0 with the diameter ratio of described reduction section 1, excellent
Elect 2-3 as；The upper port diameter of described undergauge section 2 is 0.7-1.0 with the diameter ratio of described reduction section 1,
It is preferably 0.85-0.95.
Preferably, the bottom in described reduction section 1 cavity is provided with for being distributed the described reduction section 1 of feeding
The gas distributor 13 of reducing gas.
Preferably, described gas distributor 13 be selected from single flow, lateral flow type, tubular type, bubble cap formula and
At least one form in wire netting.
Preferably, described gas-solid quick disconnector 9 is umbrella hat type, ejection type, side channel formula or T-shaped elbow
Formula gas-solid quick disconnector, preferably umbrella hat type gas-solid quick disconnector.
Preferably, the angle between periphery wall and the horizontal plane of described changeover portion 3 is more than in described extension diameter section
The angle of repose of the catalyst fines of deposition.
Preferably, it is characterised in that described offgas outlet 11 is expanding with described by dust filter unit 12
The cavity fluid UNICOM of section 4.
Second aspect present invention: providing a kind of fischer-tropsch catalysts method of reducing, the method includes: will treat also
Former fischer-tropsch catalysts is sent into reduction reactor and is carried out reduction treatment under the reducing conditions, it is characterised in that should
Method also includes: by dust separation section by described reduction reactor while carrying out described reduction treatment
In catalyst fines from reduction fischer-tropsch catalysts product separate.
Preferably, the particle diameter of described catalyst fines is less than 60 microns.
Preferably, described reduction treatment is carried out in the reduction reactor that first aspect present invention is provided.
Preferably, the condition of described reduction treatment is: temperature is 240-350 DEG C, and reduction pressure is 0.1-0.3
MPa, reduction reactor inlet velocity is 0.04-0.25 meter per second, dense fluidized district caltalyst volume concentrations
For 40-75%, reducing gas is hydrogen, carbon monoxide and/or synthesis gas.
Preferably, the condition of described reduction treatment is: temperature is 250-300 DEG C, and reduction pressure is
0.15-0.25 MPa, reduction reactor inlet velocity is 0.06-0.12 meter per second, dense fluidized district catalyst
Volumetric concentration is 55-65%, and in reducing gas, hydrogen is (5-20) with the mol ratio of carbon monoxide: 1.
The fischer-tropsch catalysts reduction reactor of present invention offer and catalyst reduction method, have the most excellent
Point:
1, the gas-liquid-solid phase reaction in slurry bed system activated reactor is converted to gas-particle two-phase reaction, carries
The mass transfer rate of high catalyst reduction reaction and reaction rate, reduce reactor scale, improve dress
The production capacity put；
2, by the design of activated reactor, by the fine powder produced during catalyst reduction and bulky grain
Catalyst is separated so that in reducing catalyst product, fine powder content reduces, and alleviates F-T synthesis
The filter pressure of reactor；
3, in reducing catalyst can be stored directly in the hermetic container of synthesis gas protection, convenient transport
And use, can be with quick-replaceable when in synthesis reactor, catalyst needs to change, organization of production is convenient.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and constitutes the part of description, with
Detailed description below is used for explaining the present invention together, but is not intended that limitation of the present invention.?
In accompanying drawing:
Fig. 1 is the structure of a kind of detailed description of the invention of the fischer-tropsch catalysts reduction reactor that the present invention provides
Schematic diagram, is also a kind of detailed description of the invention institute of the fischer-tropsch catalysts method of reducing that the present invention provides simultaneously
The structural representation of the reduction reactor used.
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 outlets
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, the detailed description of the invention of the present invention is described in detail.It should be appreciated that
Detailed description of the invention described herein is merely to illustrate and explains the present invention, is not limited to this
Bright.
First aspect present invention: provide a kind of fischer-tropsch catalysts reduction reactor, it is characterised in that described
Reduction reactor include the upper end one of columnar reduction section 1 and described reduction section 1 be connected and with institute
State the coaxial undergauge section 2 of reduction section 1 and by the expansion bigger than described reduction section 1 of changeover portion 3 and diameter
The lower end of the dust separation section that footpath section 4 is integrally formed, the lower end of described changeover portion 3 and described undergauge section 2
Outer surface is tightly connected so that described undergauge section 2 is 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, and the bottom of reduction section 1 sets
Being equipped with reducing gas entrance 6, the bottom of reduction section 1 is provided with reducing catalyst outlet 7；Described undergauge
The top of section 2 be provided with for send catalyst fines and the undergauge section gas outlet 8 of reduction tail gas and
It is positioned at the gas-solid quick disconnector 9 above described undergauge section gas outlet 8 relative spacing；Described transition
The bottom of section 3 is provided with catalyst fines outlet 10；It is provided with on the top sealing plate of described extension diameter section 4
For sending the offgas outlet 11 of reduction tail gas.
According to the first aspect of the invention, described fischer-tropsch catalysts to be restored and fischer-tropsch catalysts are abilities
Known to field technique personnel, can be graininess, microspheroidal or powdery, preferably metal Fischer-Tropsch catalytic
Agent, more preferably iron-base fischer-tropsch synthesis catalyst.
According to the first aspect of the invention, described reduction reactor refers to for reducing the anti-of fischer-tropsch catalysts
Answer device, can be Dual-Phrase Distribution of Gas olid fluidized bed reactor or internal recycling zero gradient reactor, be preferably fixing stream
Fluidized bed reactor.
According to the first aspect of the invention, the ratio of height to diameter of described reduction section 1 can be 3-10, is preferably
4-8, more preferably 5-6；The ratio of height to diameter of described extension diameter section 4 can be 2-6, preferably 3-4；Described expansion
The diameter of footpath section 4 can be 1.5-5.0, preferably 2-3 with the diameter ratio of described reduction section 1；Described
The upper port diameter of undergauge section 2 can be 0.7-1.0 with the diameter ratio of described reduction section 1, is preferably
0.85-0.95。
According to the first aspect of the invention, gas-solid quick disconnector can be utilized in described dust separation section
9 and granule sedimentation separate the fine powder that described reduction tail gas is carried secretly, and fine powder is by described dust separation section
Bottom discharge reduction reactor, the particle size range isolating fine powder can be below 60 μm, be preferably
Below 50 μm, more preferably below 30 μm.Described gas-solid quick disconnector is art technology
Known to personnel, for example, it is possible to be that umbrella hat type, ejection type, side channel formula or T-shaped elbow type gas-solid are fast
Speed separator, preferably umbrella hat type gas-solid quick disconnector.Wherein, the gas-solid of described umbrella hat type quickly divides
Beeline from device with described undergauge section gas outlet 8 can be 1-2 times of described undergauge section 2 diameter.
According to the first aspect of the invention, the angle between perisporium and the horizontal plane of described changeover portion 3 is the least
In described extension diameter section, the angle of repose of the catalyst fines of deposition, described angle of repose is those skilled in the art
Known, refer in gravitational field, suffered gravity when particle slides on the free inclined-plane of powder body accumulation horizon
With frictional force reaches balance and the maximum angular that records of remaining static down between particle.
According to the first aspect of the invention, the bottom in described reduction section 1 cavity can be provided with for dividing
The gas distributor 13 of the reducing gas of described reduction section 1 sent into by cloth；The height of described gas distributor 13
Degree can export 7 less than described reducing catalyst.Wherein, described gas distributor is people in the art
Known to Yuan, can be in single flow, lateral flow type, tubular type, bubble cap formula and wire netting at least
A kind of form, preferably tubular type and/or emit bubble, more preferably tubular type.
According to the first aspect of the invention, described offgas outlet 11 can pass through dust filter unit 12 and institute
State the cavity fluid UNICOM of extension diameter section 4.Described dust filter unit is well-known to those skilled in the art,
May be used for filtering the catalyst fines not settled in reduction tail gas, described pneumatic filter is preferably with efficiently
The filter of low pressure drop, to reduce the overall pressure drop of reduction reactor system, reduces power consumption.
According to the first aspect of the invention, described reducing catalyst outlet 7 can pass through catalyst emission pipe
Road 14 connects with reducing catalyst after-treatment system；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 pass through fine powder discharge pipe 15 and catalyst
Fine powder processing system connects；Stop not less than catalyst fines in the inclination angle of described fine powder discharge pipe 15
Angle.
Second aspect present invention: providing a kind of fischer-tropsch catalysts method of reducing, the method includes: will treat also
Former fischer-tropsch catalysts is sent into reduction reactor and is carried out reduction treatment under the reducing conditions, it is characterised in that should
Method also includes: by dust separation section by described reduction reactor while carrying out described reduction treatment
In catalyst fines from reduction fischer-tropsch catalysts product separate.Wherein said catalyst fines
Particle diameter can be below 60 μm, below preferably 50 μm, more preferably below 30 μm.
A kind of detailed description of the invention according to a second aspect of the present invention, described reduction treatment can be in the present invention
The reduction reactor that first aspect is provided is carried out.
According to the second aspect of the invention, described reduction treatment is well-known to those skilled in the art, its
Condition can be: temperature is 240-350 DEG C, and reduction pressure is 0.1-0.3 MPa, reduction reactor entrance
Linear speed is 0.04-0.25 meter per second, and dense fluidized district caltalyst volume concentrations is 40-75%, and reducing gas is
Hydrogen, carbon monoxide and/or synthesis gas.The condition of described reduction treatment is preferably: temperature is 250-300 DEG C,
Reduction pressure is 0.15-0.25 MPa, and reduction reactor inlet velocity is 0.06-0.12 meter per second, dense-phase flow
Changing district's caltalyst volume concentrations is 55-65%, and in reducing gas, hydrogen with the mol ratio of carbon monoxide is
(5-20): 1, wherein said synthesis gas is well-known to those skilled in the art containing hydrogen with an oxygen
Change the gas of carbon.
The present invention will be further illustrated by embodiment below, but the most therefore the present invention will be taken office
What limits.The catalyst grain size distribution of the embodiment of the present invention uses GB/T 19077.1-2003 method to carry out
Measure.
Embodiment 1:
As shown in Figure 1: in the activated reactor that expanding ratio is 2, add catalyst 1kg to be restored, use
Air in activation system is replaced completely by nitrogen at normal temperatures and pressures, with H2: the reducing gases of CO=20:1
Body composition is passed through reducing gases to going back original system, makes the pressure of priming reaction system be increased to 0.1MPa, rises
Maintain gas empty tower gas velocity 0.06m/s constant during pressure.Then according to reduction activation heating curve is by reactor
Heat temperature raising, carries out constant temperature reductase 12 0h, dense fluidized district catalyst volume at 260 DEG C to catalyst
Concentration is between 65-70%.After reduction terminates, keep activation system reducing gas air speed and reduction pressure
Constant, stopped reaction device heats, and temperature of reactor to be restored is down to 50 DEG C, catalyst is entered synthesis gas
In hermetic container under Bao Hu, become product for synthesis technique.
Weighing catalyst bulky grain and the weight of fine powder respectively, bulky grain accounting is 96.44%, and fine powder accounts for
Ratio is 1.80%, loses 1.76%.Application laser particle analyzer to untreated catalyst, catalyst bulky grain,
The granularmetric composition of catalyst fines is analyzed, and is shown in Table 1.
As shown in table 1, catalyst is after reduction activation, and catalyst pellets radially moves in small particles direction,
And occur in that a number of fine powder；Described reduction activation device can preferably remove activation of catalyst
During the fine powder that produces, keep the oarse-grained particle size distribution of catalyst and untreated catalyst basic
Cause.By regulation reducing gas empty tower gas velocity, can make further the oarse-grained particle size distribution of catalyst with
Untreated catalyst is completely the same.I.e. can be thin by what fine powder in catalyst raw material and reduction process produced
Powder is removed in the lump so that the catalyst entering synthesis reactor is bulky grain, reduces synthesis reactor
Filter pressure, improves the parallel-adder settle-out time of synthesis reactor.
The particle 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, use
Air in activation system is replaced completely by nitrogen at normal temperatures and pressures, with H2: the reducing gas of CO=5:1
Form and be passed through reducing gases to going back original system, make the pressure of priming reaction system be increased to 0.2MPa, boosting
Time maintain gas empty tower gas velocity 0.2m/s constant.Then according to reactor is added by reduction activation heating curve
Heat heats up, and catalyst carries out at 300 DEG C constant temperature reduction 12h, and dense fluidized district catalyst volume is dense
Between degree is for 55-60%.After reduction terminates, keep activation system reducing gas air speed and reduction pressure not
Becoming, stopped reaction device heats, and temperature of reactor to be restored is down to 80 DEG C, catalyst enters synthesis gas and protects
In hermetic container under protecting, become product for synthesis technique.
Weighing catalyst bulky grain and the weight of fine powder respectively, bulky grain accounting is 97.97%, and fine powder accounts for
Ratio is 0.91%, loses 1.12%.Application laser particle analyzer to untreated catalyst, catalyst bulky grain,
The granularmetric composition of catalyst fines is analyzed, and is shown in Table 2.
As shown in table 2, catalyst is after reduction activation, and catalyst pellets radially moves in small particles direction,
And occur in that a number of fine powder；Described reduction activation device can preferably remove activation of catalyst
During the fine powder that produces, keep the oarse-grained particle size distribution of catalyst and untreated catalyst basic
Cause.By regulation reducing gas empty tower gas velocity, can make further the oarse-grained particle size distribution of catalyst with
Untreated catalyst is completely the same.I.e. can be thin by what fine powder in catalyst raw material and reduction process produced
Powder is removed in the lump so that the catalyst entering synthesis reactor is bulky grain, reduces synthesis reactor
Filter pressure, improves the parallel-adder settle-out time of synthesis reactor.
The particle size distribution of table 2 catalyst
Claims (14)
1. a fischer-tropsch catalysts reduction reactor, it is characterised in that
Described reduction reactor includes columnar reduction section (1) and the upper end of described reduction section (1)
One connects and the undergauge section (2) coaxial with described reduction section (1) and by changeover portion (3) and directly
The dust separation section that the footpath extension diameter section (4) bigger than described reduction section (1) is integrally formed, described changeover portion
(3) lower end is tightly connected so that described undergauge section (2) with the lower end outer surface of described undergauge section (2)
It is 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 also
Raw catalyst outlet (7)；The top of described undergauge section (2) be provided with for send catalyst fines and
Reduction undergauge section gas outlet (8) of tail gas and relative spacing ground are positioned at described undergauge section gas outlet
(8) the gas-solid quick disconnector (9) of top；
The bottom of described changeover portion (3) is provided with catalyst fines outlet (10)；
The offgas outlet for sending reduction tail gas it is provided with on the top sealing plate of described extension diameter section (4)
(11)。
Reduction reactor the most according to claim 1, it is characterised in that described reduction reactor is gas
Fixed double phase flow fluidized bed reactor or internal recycling zero gradient reactor, preferably fixed fluidized-bed reactor.
Reduction reactor the most according to claim 1, it is characterised in that the height of described reduction section (1)
Footpath is than for 3-10, and the ratio of height to diameter of described extension diameter section (4) is 2-6.
Reduction reactor the most according to claim 1, it is characterised in that described extension diameter section (4) straight
Footpath is 1.5-5.0, preferably 2-3 with the diameter ratio of described reduction section (1)；Described undergauge section (2)
The diameter ratio of upper port diameter and described reduction section (1) be 0.7-1.0, preferably 0.85-0.95.
Reduction reactor the most according to claim 1, it is characterised in that described reduction section (1) cavity
Interior bottom is provided with the gas distributor for being distributed the reducing gas sending into described reduction section (1)
(13)。
Reduction reactor the most according to claim 5, it is characterised in that described gas distributor (13)
For at least one form in single flow, lateral flow type, tubular type, bubble cap formula and wire netting.
Reduction reactor the most according to claim 1, it is characterised in that described gas-solid quick disconnector
(9) it is umbrella hat type, ejection type, side channel formula or T-shaped elbow type gas-solid quick disconnector, preferably umbrella crown
Formula gas-solid quick disconnector.
Reduction reactor the most according to claim 1, it is characterised in that outside described changeover portion (3)
Angle between perisporium and horizontal plane is more than the angle of repose of the catalyst fines of deposition in described extension diameter section.
Reduction reactor the most according to claim 1, it is characterised in that described offgas outlet (11)
Cavity fluid UNICOM by dust filter unit (12) Yu described extension diameter section (4).
10. a fischer-tropsch catalysts method of reducing, the method includes: sent into by fischer-tropsch catalysts to be restored
Reduction reactor carries out reduction treatment under the reducing conditions, it is characterised in that the method also includes: entering
By dust separation section by the catalyst fines in described reduction reactor while the described reduction treatment of row
Separate from reduction fischer-tropsch catalysts product.
11. methods according to claim 10, wherein, the particle diameter of described catalyst fines is 60 microns
Below.
12. methods according to claim 10, wherein, described reduction treatment is according to claim 1-9
Reduction reactor described in middle any one is carried out.
13. methods according to claim 10, wherein, the condition of described reduction treatment is: temperature is
240-350 DEG C, reduction pressure be 0.1-0.3 MPa, reduction reactor inlet velocity be 0.04-0.25 rice/
Second, dense fluidized district caltalyst volume concentrations is 40-75%, reducing gas be hydrogen, carbon monoxide and/
Or synthesis gas.
14. methods according to claim 10, wherein, the condition of described reduction treatment is: temperature is
250-300 DEG C, reduction pressure is 0.15-0.25 MPa, and reduction reactor inlet velocity is 0.06-0.12 rice
/ the second, dense fluidized district caltalyst volume concentrations is 55-65%, hydrogen and carbon monoxide in reducing gas
Mol ratio is (5-20): 1.
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