CN1814350A - Industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst - Google Patents
Industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst Download PDFInfo
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- CN1814350A CN1814350A CNA2005100269682A CN200510026968A CN1814350A CN 1814350 A CN1814350 A CN 1814350A CN A2005100269682 A CNA2005100269682 A CN A2005100269682A CN 200510026968 A CN200510026968 A CN 200510026968A CN 1814350 A CN1814350 A CN 1814350A
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Abstract
This invention relates to an industrial reducing method of granular iron base fei tuo synthetic catalyst. The method is a catalyst reducing process independent of fei tuo synthetic catalyst. The reducing process is separated to reducing stage and adjusting stage, they react in a independent reactor, operation temperature is 260-450 degree centigrade, pressure is 1.5-5.0MPa, entrance linear speed is 0.15-0.7 m/s,the catalyst volume concentration at fluidized bed dense phase area is 5-60%. Reducing gas is H<SUB>2</SUB> or CO, or mixed gas of H<SUB>2</SUB>and CO. the reducing technological process includes following equipment: compressor, heating and heat exchanger, cooling heat exchanger, reducing reactor, dust collector, steam and liquor separator, catalyst reducing charge chute and catalyst charge chute.
Description
Technical field
The present invention relates to a kind of industrial reduction method of iron-base fischer-tropsch synthesis catalyst, the catalyst that this method obtains will be used for industrial reactor, as carrying out Fischer-Tropsch synthesis in the fluidized-bed reactor.
Background technology
The Fischer-Tropsch building-up process is utilized synthesis gas, reacts in reactor under the effect of catalyst and uniform temperature, pressure, generates a series of hydrocarbon compound.The Fischer-Tropsch building-up process can be divided into high temperature fischer-tropsch building-up process and low temperature Fischer-Tropsch building-up process with the difference of reaction temperature.For the high temperature fischer-tropsch building-up process, its reactor generally adopts fluidized-bed reactor, and short hydrocarbon is more in the product; The reactor of low temperature Fischer-Tropsch building-up process then mainly adopts paste state bed reactor, and long chain hydrocarbon is more in the product.Two kinds of processes differ from one another, and select which kind of process to depend primarily on the purpose product.
The synthetic used catalyst of Fischer-Tropsch has multiple, and commonly used be iron-based or cobalt-base catalyst, and ferrum-based catalyst is owing to less expensive, thereby has obtained extensive use in the Fischer-Tropsch building-up process.
After need reducing, iron-base fischer-tropsch synthesis catalyst just has activity, in existing bibliographical information and patent, the reduction of iron-base fischer-tropsch synthesis catalyst is carried out in the Fischer-Tropsch synthesis device, come reducing catalyst according to certain inlet gas composition, temperature, pressure and air speed, the synthetic reactivity of Fischer-Tropsch is stablized gradually with the raising of reducing degree, switches to synthetic state after reduction is finished.More than report is generally the process of carrying out in the laboratory.
In application number is 03151105.8 patent, a kind of industrial reduction method that is used for the iron-base fischer-tropsch synthesis catalyst of paste state bed reactor has been proposed, point out: for industrial paste state bed reactor, if building-up process and reduction process are carried out in same reactor, maximum problem is the online updating and the reduction of catalyst.Catalyst begin the Fischer-Tropsch building-up process after reduction is finished first, after operation a period of time, catalyst is inactivation gradually, needs to add new catalyst and replace the part catalyst.Reduce if directly catalyst is added in the synthesis reactor, since the catalyst that adds be in the very high state of moisture (in this moment reactor dividing potential drop of water may account for stagnation pressure 20%), to cause reducing insufficient, and cause the sintering and the fragmentation of catalyst easily.If use high H
2The gas of/CO ratio restores after system is replaced, and then needs to spend considerable time to carry out, and has caused the interruption of building-up process, and the Fischer-Tropsch synthetic space-time yield sharply descends.The commercial plant of large-scale continuous production obviously can not be operated in this way.So the syrup state bed Fischer Tropsch for industry is synthetic, should dispose independently a reduction reactor and a supporting reduction unit thereof.
Though above-identified patent at be low temperature Fischer-Tropsch building-up process, in the high temperature fischer-tropsch building-up process, also exist same problem, need take measures with catalyst activity the best of guaranteeing newly to add.
Summary of the invention
Purpose of the present invention just provide a kind of independently, the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst that reducing degree is high, the catalyst that this method reduction obtains will be used for industrial reactor, as carrying out Fischer-Tropsch synthesis in the fluidized-bed reactor, but the synthesis reactor form is not limited to fluidized-bed reactor.
Purpose of the present invention can be achieved through the following technical solutions: the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst is characterized in that this method comprises following processing step:
(1) ferrum-based catalyst is added the catalyst charge groove, the mode of catalyst being carried with dilute phase by gases at high pressure is sent in the reduction reactor of fluid bed form again;
(2) by compressor reducing gas is pressed in the reduction reactor and carries out reduction reaction with catalyst, the reduction reactor operating temperature is 260～450 ℃, pressure is 2.0～5.0MPa, the inlet linear speed is 0.15～0.7m/s, fluid bed emulsion zone caltalyst volume concentrations is 5～60%, and the reduction reaction process comprises reduction phase and two stages of adjusting stage;
(3) mode of carrying with dilute phase by gases at high pressure will reduce good catalyst to be depressed in the catalyst charge groove storage stand-by;
Realize at least one cooling heat exchanger, at least one dust arrester being set, at least one gas-liquid separator above processing step need be provided with at least one compressor, at least one heating heat exchanger, at least one heating furnace, reduction reactor outlet before the reduction reactor inlet after.
The reduction phase of described reduction reaction can be supplied with and add heat, and to keep reduction temperature, the temperature that is masked as reduction reactor of end begins to continue to rise, and this time in stage is 12～24h.
The adjusting stage of described reduction reaction carries out after reduction phase, removable reaction heat of this stage, and the temperature that is masked as reduction reactor of end and the outlet of gas composition tend towards stability, and this time in stage is 24～48h.
The reduction of described catalyst is carried out in the reduction reactor that is independent of the Fischer-Tropsch synthesis device, and this reduction reactor is a fluidized-bed reactor.
Described catalyst reduction charge chute is provided with at least one, this groove pressure is controlled by the aperture of regulating reduction charge chute atmospheric valve and reduction charge chute gases at high pressure adding valve, catalyst passes through the Valved discharge of bottom in the gases at high pressure pipeline, is transported to reduction reactor by the gases at high pressure pipeline; The charging rate of catalyst is controlled by reduction charge chute and the differential pressure of reduction reactor and/or the aperture of baiting valve, by regulating the gases at high pressure flow, makes the material gas weight ratio of conveying, and promptly catalyst and gases at high pressure carry the ratio of weight flow between 1～20.
It is uniform that described reduction reactor inside has distribution device in gas-fluid that gas is carried out, and have the gases at high pressure blow line to handle the distributor obstruction on the suction line; The reactor middle part has cold pipe of heat exchange and heater to remove or provide heat; Reactor head has gas-solid separating device.
Described reduction reactor is in the operation cycle, and the exit gas at reduction reactor top is cooled to enter gas-liquid separator then near room temperature through cooling heat exchanger through the catalyst granules of dust arrester except that deentrainment.
Described reduction reactor is in the operation cycle, the exit gas at reduction reactor top is after dust arrester removes the catalyst granules of deentrainment, in the one-level gas-liquid separator partially liq is collected after the cooling of one-level cooler earlier, gas removes the secondary gas-liquid separator through secondary coolers again.
The liquid of described gas-liquid separator separates discharges as reaction water; The discharging of a gas part, a part mix the back as circulating air and use compressor boost with fresh supply gas, send to the preceding preheater inlet of reactor.
The reduction phase of described reduction reaction, reducing gases be through after heating heat exchanger is preheating to uniform temperature, is heated to temperature requiredly again by heating furnace, sends into reduction reactor at last, and this moment, the by-pass bypass valve was generally closed; Provide reaction required heat by gas-fired heater mode or Electric heating again at the reduction reactor body.
The adjusting stage of described reduction reaction, reduction reactor progressively reduces the outer heating load of reactor with the increase of this stage reducing degree, can realize by the heating and/or the multiple mode of cooling load of conditioned reaction device inlet temperature and/or reduction reactor.
The adjusting of described reactor inlet temperature can be regulated charging heating heat exchanger main line valve and cooling by-pass bypass valve aperture by regulating the heating furnace thermic load that enters the mouth, and reduces means realizations such as heating heat exchanger thermic load.
The heating of described reduction reactor and/or the adjusting of cooling load realize by cold pipe boiler feedwater feeding amount of heat exchange in the conditioned reaction device and heater thermic load.
Described reduction reactor adds valve by the reactor gases at high pressure of regulating the top and comes conditioned reaction device pressure behind complete and continuous reduction cycle of experience; The Valved discharge that passes through the bottom with catalyst when needs discharge is transported to reduction reactor by the gases at high pressure dilute phase in the gases at high pressure pipeline; The charging rate of catalyst leans on the charge chute and the differential pressure of reduction reactor and/or the aperture of baiting valve to be controlled, and by regulating the gases at high pressure flow, makes the material gas weight ratio of conveying, and promptly catalyst and gases at high pressure carry the ratio of weight flow between 1～20.
Described catalyst charge groove is established heat(ing) coil, causes too violent thermal perturbation in order to avoid catalyst temperature hangs down very much when adding synthesis reactor, regulates pressure by the aperture of regulating charge chute gases at high pressure adding valve and charge chute atmospheric valve; When synthesis reactor need be added catalyst, catalyst is sent in the synthesis reactor with thermal high gas.
Described reducing gas can be H
2Or CO, also can be H
2Mist with CO.
Described gases at high pressure can be high-pressure inert gas such as nitrogen, also can be high-pressure process gas such as reducing gas.
If adopt H
2With the reduction of the mist of CO, the required reducing condition of fischer-tropsch synthetic catalyst is different with the synthesis condition of Fischer-Tropsch synthesis device, the H that building-up process is required
2/ CO is lower.If reduce under synthesis condition, along with the increase on catalyst activity surface, Fischer-Tropsch synthesis begins to carry out on the catalyst, generates a large amount of moisture.Prove that according to existing bibliographical information and experimental study the increase of moisture will have following influence to ferrum-based catalyst: with the cementite with activity of generation after the catalyst surface reduction or the oxide that elemental iron is oxidized to non-activity; Thereby insufficient catalyst activity that makes that causes reducing is lower; Promote the sintering of catalyst; Cause the fragmentation of catalyst.
Compared with prior art, the industrial reduction method of iron-base fischer-tropsch synthesis catalyst of the present invention is an independently reduction process, and this reduction process is a batch process, and the catalyst after the reduction adds synthesis reactor as required.Because reduction process and building-up process are two independently processes, can adopt higher H in reduction process
2/ CO ratio has effectively reduced the influence of the moisture of reduction later stage Fischer-Tropsch synthesis generation for reducing catalyst.
As previously mentioned, for iron-base fischer-tropsch synthesis catalyst, the reduction process of catalyst can successively be divided into reduction phase and two stages of adjusting stage.At reduction phase, main what take place is that partial oxidation iron contained in the catalyst is reduced to the iron atom with catalytic activity and the endothermic reaction of cementite; And,, begin to have the Fischer-Tropsch synthesis of heat release on catalyst, to take place along with the raising of catalyst reduction degree in the adjusting stage, and rate of heat release surpassed the heat absorption rate of catalyst activity composition reduction, and aggregate performance is exothermic reaction.The different phase that the present invention is directed to reduction has been determined different process conditions, to obtain best catalyst activity.
For industrial reactor, because each additional amount different and different with catalyst and service condition, independently the catalytic amount that reduces in the reduction unit is identical with additional amount.Simultaneously, the catalyst that reduction is good can carry out online updating, can guarantee the long synthetic operation cycle like this, realizes the long-term and stable production of Fischer-Tropsch building-up process.In addition,, can carry out synchronously, avoid the interruption of building-up process with synthetic because reduction is independently.
Because the catalyst of this flow process adopts high-pressure inert gas dilute phase strength to carry rather than carry with pump, has reduced the breakage of catalyst in transmission effectively.
Description of drawings
Fig. 1 is the Fischer-Tropsch synthetic iron-based catalyst reducing process flow chart of an industrial intermediate experiment.
The specific embodiment
Embodiment 1
As shown in Figure 1, fresh raw catalyst adds catalyst reduction charge chute 37 by catalyst charging hopper 22.After catalyst adds, open reduction charge chute baiting valve 21, catalyst enters the high pressure nitrogen pipeline of bottom, delivers into reduction reactor 15 by high pressure nitrogen.The pressure of catalyst reduction charge chute 37 is kept by the aperture that adjusting reduction charge chute atmospheric valve 23 and reduction charge chute nitrogen add valve 24, with the pressure reduction of reactor maintenance 2bar, guarantees the certain transporting velocity of catalyst when the catalyst gas-phase transport.The flow of high pressure nitrogen is regulated by high pressure nitrogen control valve 20, pass through the pressure reduction of reduction charge chute 37 and reduction reactor 15 like this, material gas weight ratio when the flow of high pressure nitrogen guarantees to carry is about 5, transporting velocity is that the loadings of 4m/s. catalyst is 500kg, closes reduction charge chute baiting valve 21. after catalyst adds fully
The whole process of catalyst reduction is as follows: after with hydrogen being compressed machine 3 compression superchargings of the reducing gases of main component and heating heat exchanger 4, heating furnace 8 heat exchange, entering reduction reactor 15 and reduce under certain temperature and pressure.The exit gas of reduction reactor 15 is through dust arrester 26 dedustings, by 27 coolings of reduction cooler, liquid reclaims in High Temperature Gas liquid/gas separator 28, gas enters in the gas-liquid separator 30 after cooling heat exchanger 29 is cooled to normal temperature again, liquid after the separation is sent to reaction water treatment, uncooled most of gas mixes with virgin gas after reduce after recycle compressor 3 pressurization, returns the reduction reactor inlet.
The gas access linear speed of reduction reactor 15 is 0.45m/s.Reduction temperature is 400 ℃, and operating pressure is 3.0MPa.Reduction reactor 15 is mainly realized by conditioned reaction gas access temperature with the mean temperature of bed.At the reduction phase of catalyst reduction, be main by regulating heating heat exchanger 4 thermic loads, the aperture of adjusting heating furnace 8 thermic loads, heating heat exchanger main line valve 6 and cooling by-pass valve 5 is the control that the mode of assisting realizes the reduction reactor inlet temperature.At first need to open big heating furnace by-pass control valve 10 apertures gradually in the adjusting stage of catalyst reduction, and reduce heating furnace 8 thermic loads gradually, finally stop heating furnace 8, close the inlet valve 7 and the outlet valve 9 of heating furnace 8 according to the variation of temperature of reactor; Mainly regulate temperature then, regulate the thermic load of electric heater 16 and the aperture of the boiler water valve 19 that is used to cool off in case of necessity by the aperture of regulating heating heat exchanger main line valve 6 and cooling by-pass valve 5.
After gas enters reduction reactor 15, undertaken by built-in gas distributor 38 uniform, even with the fluidisation that realizes gas in the bed.The inlet of reduction reactor 15 is provided with an accident nitrogen treatment pipeline 11, purges when stopping up appears in gas distributor by this pipeline.The middle part of fluid bed is provided with cold pipe 17 and electric heater 16, can effectively remove and provide heat to reactor.Reactor top is built-in with gas-solid separating device 18, and the most catalyst traps that gas can be carried secretly are got off.
Reduction reactor 15 exit gas further remove the catalyst of carrying secretly through dust arrester 26 earlier, enter reduction one-level cooler 27 again and be cooled to 130 ℃, enter High Temperature Gas liquid/gas separator 28 then with the separating high-temp condensed fluid, gas phase is cooled to 40 ℃ through reduction secondary coolers 29 again and enters gas-liquid separator 30 separation again, after coming out from the top, mixes gas with virgin gas, enter reduction recycle compressor 3 then and compress, send to reduction reactor 15 suction lines.
After catalyst reduction is good, reduction unit is carried out shut-down operation.After the parking of confirming reduction unit is finished, open reduction reactor bottom baiting valve 12 and reduction reactor bottom baiting valve 14, catalyst enters the high pressure nitrogen pipeline of bottom, delivers into catalyst charge groove 31 by high pressure nitrogen.This moment, the pressure of reduction reactor 15 was kept by the aperture of regulating reduction reactor top atmospheric valve 25 and reduction reactor nitrogen adding valve 39, with the pressure reduction of catalyst charge groove maintenance 2bar, guarantee the certain transporting velocity of catalyst when the catalyst gas-phase transport.The flow of high pressure nitrogen is regulated by high pressure nitrogen control valve 13, and by the pressure reduction of reduction reactor 15 and catalyst charge groove 31, the material gas weight ratio the when flow of high pressure nitrogen guarantees to carry is about 5 like this, and transporting velocity is 4m/s.
The pressure of catalyst charge groove 14 adds valve 33 by control charge chute atmospheric valve 32 and charge chute high pressure nitrogen and keeps.Catalyst charge groove 31 guarantees certain temperature by heat(ing) coil 34 in the charge chute in order to avoid cause bigger thermal perturbation when adding synthesis reactor.On blow-down pipe, also be provided with a filter 40, be used to reduce the amount that catalyst entrainment goes out system.When needing to carry catalyst, open catalyst charge trench bottom baiting valve 35, catalyst enters the high pressure nitrogen pipeline of bottom, delivers into synthesis reactor by high pressure nitrogen.The flow of high pressure nitrogen is regulated by high pressure nitrogen control valve 36.
According to above-mentioned technology 8 batches of catalyst of coreduction at first, the catalyst that reduction is good pursues criticizes the synthesis reactor of packing into, in building-up process, one week was carried out the online updating of a catalyst, promptly discharge a certain amount of old catalyst, replenish the good fresh catalyst of reduction of equivalent amount and concentration again, with average activity, selectivity and the catalyst loading of regular recovery catalyst in reactor.At 400 ℃, 3.0MPa, the inlet linear speed is under the synthesis condition of 0.45m/s, CO and CO
2Total conversion maintain all the time more than 80%, the above components selection of C5 is more than 50%.
Embodiment 2
Substantially the same manner as Example 1, difference is the operating condition of reduction process: the arrival line speed control is made as 0.15m/s, and the temperature of reduction phase and adjusting stage is 330 ℃, and operating pressure is 4.7MPa, and all the other operating conditions are constant.Under the synthesis condition identical with embodiment 1, catalyst after the reduction still carries out one time online updating a week, and the result shows that total conversion slightly descends under this operating condition, but still can maintain 75～80% level, the above component selectivity of C5 is also more than 50%.
Claims (17)
1. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst is characterized in that, this method comprises following processing step:
(1) ferrum-based catalyst is added the catalyst charge groove, the mode of catalyst being carried with dilute phase by gases at high pressure is sent in the reduction reactor of fluid bed form again;
(2) by compressor reducing gas is pressed in the reduction reactor and carries out reduction reaction with catalyst, the reduction reactor operating temperature is 260～450 ℃, pressure is 2.0～5.0MPa, the inlet linear speed is 0.15～0.7m/s, fluid bed emulsion zone caltalyst volume concentrations is 5～60%, and the reduction reaction process comprises reduction phase and two stages of adjusting stage;
(3) mode of carrying with dilute phase by gases at high pressure will reduce good catalyst to be depressed in the catalyst charge groove storage stand-by;
Realize at least one cooling heat exchanger, at least one dust arrester being set, at least one gas-liquid separator above processing step need be provided with at least one compressor, at least one heating heat exchanger, at least one heating furnace, reduction reactor outlet before the reduction reactor inlet after.
2. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, the reduction phase of described reduction reaction, can supply with and add heat, to keep reduction temperature, the temperature that is masked as reduction reactor that finishes begins to continue to rise, and this time in stage is 12～24h.
3. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, the adjusting stage of described reduction reaction carries out after reduction phase, removable reaction heat of this stage, temperature that is masked as reduction reactor that finishes and the outlet of gas composition tend towards stability, and this time in stage is 24～48h.
4. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that: the reduction of described catalyst is carried out in the reduction reactor that is independent of the Fischer-Tropsch synthesis device, and this reduction reactor is a fluidized-bed reactor.
5. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, described catalyst reduction charge chute is provided with at least one, this groove pressure is controlled by the aperture of regulating reduction charge chute atmospheric valve and reduction charge chute gases at high pressure adding valve, catalyst passes through the Valved discharge of bottom in the gases at high pressure pipeline, is transported to reduction reactor by the gases at high pressure pipeline; The charging rate of catalyst is controlled by reduction charge chute and the differential pressure of reduction reactor and/or the aperture of baiting valve, by regulating the gases at high pressure flow, makes the material gas weight ratio of conveying, and promptly catalyst and gases at high pressure carry the ratio of weight flow between 1～20.
6. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, it is uniform that described reduction reactor inside has distribution device in gas-fluid that gas is carried out, and have the gases at high pressure blow line to handle the distributor obstruction on the suction line; The reactor middle part has cold pipe of heat exchange and heater to remove or provide heat; Reactor head has gas-solid separating device.
7. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, described reduction reactor is in the operation cycle, the exit gas at reduction reactor top is cooled to enter gas-liquid separator then near room temperature through cooling heat exchanger through the catalyst granules of dust arrester except that deentrainment.
8. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, described reduction reactor is in the operation cycle, the exit gas at reduction reactor top is after dust arrester removes the catalyst granules of deentrainment, in the one-level gas-liquid separator partially liq is collected after the cooling of one-level cooler earlier, gas removes the secondary gas-liquid separator through secondary coolers again.
9. according to the industrial reduction method of claim 7 and 8 described particle iron-base fischer-tropsch synthesis catalysts, it is characterized in that the liquid of described gas-liquid separator separates discharges as reaction water; The discharging of a gas part, a part mix the back as circulating air and use compressor boost with fresh supply gas, send to the preceding preheater inlet of reactor.
10. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 2, it is characterized in that, the reduction phase of described reduction reaction, reducing gases is after being preheating to uniform temperature through heating heat exchanger, be heated to temperature required again by heating furnace, send into reduction reactor at last, this moment, the by-pass bypass valve was generally closed; Provide reaction required heat by gas-fired heater mode or Electric heating again at the reduction reactor body.
11. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 3, it is characterized in that, the adjusting stage of described reduction reaction, reduction reactor progressively reduces the outer heating load of reactor with the increase of this stage reducing degree, can realize by the heating and/or the multiple mode of cooling load of conditioned reaction device inlet temperature and/or reduction reactor.
12. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 11, it is characterized in that, the adjusting of described reactor inlet temperature can be by regulating inlet heating furnace thermic load, regulate charging heating heat exchanger main line valve and cooling by-pass bypass valve aperture, reduce means realizations such as heating heat exchanger thermic load.
13. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 11, it is characterized in that, the heating of described reduction reactor and/or the adjusting of cooling load realize by cold pipe boiler feedwater feeding amount of heat exchange in the conditioned reaction device and heater thermic load.
14. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, described reduction reactor adds valve by the reactor gases at high pressure of regulating the top and comes conditioned reaction device pressure behind complete and continuous reduction cycle of experience; The Valved discharge that passes through the bottom with catalyst when needs discharge is transported to reduction reactor by the gases at high pressure dilute phase in the gases at high pressure pipeline; The charging rate of catalyst leans on the charge chute and the differential pressure of reduction reactor and/or the aperture of baiting valve to be controlled, and by regulating the gases at high pressure flow, makes the material gas weight ratio of conveying, and promptly catalyst and gases at high pressure carry the ratio of weight flow between 1～20.
15. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1, it is characterized in that, described catalyst charge groove is established heat(ing) coil, when adding synthesis reactor, cause too violent thermal perturbation in order to avoid catalyst temperature hangs down very much, regulate pressure by the aperture of regulating charge chute gases at high pressure adding valve and charge chute atmospheric valve; When synthesis reactor need be added catalyst, catalyst is sent in the synthesis reactor with thermal high gas.
16. the industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst according to claim 1 is characterized in that, described reducing gas can be H
2Or CO, also can be H
2Mist with CO.
17. the industrial reduction method according to claim 5 or 6 or 14 or 15 described particle iron-base fischer-tropsch synthesis catalysts is characterized in that, described gases at high pressure can be high-pressure inert gas such as nitrogen, also can be high-pressure process gas such as reducing gas.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106311361A (en) * | 2015-06-24 | 2017-01-11 | 神华集团有限责任公司 | System and method for activation and online renewing of catalyst |
| 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 |
| CN114345340A (en) * | 2022-01-08 | 2022-04-15 | 安庆市长虹化工有限公司 | Preparation process and working system of carrier copper nanotube dehydrogenation catalyst |
| US11629293B2 (en) | 2020-03-10 | 2023-04-18 | Yankuang Energy R&D Co., Ltd., Shanghai | System for producing hydrocarbons by high-temperature Fischer-Tropsch synthesis |
| WO2023092377A1 (en) * | 2021-11-25 | 2023-06-01 | 国家能源投资集团有限责任公司 | Method and device for continuous operation of fischer-tropsch synthesis catalyst |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1233461C (en) * | 2003-09-22 | 2005-12-28 | 上海兖矿能源科技研发有限公司 | Industrial reduction method for catalyst of Fischer-Tropsch synthesis in use for reactor in slurry state bed |
| CN1247305C (en) * | 2004-03-19 | 2006-03-29 | 中国科学院山西煤炭化学研究所 | Method for deoxidizing iron base catalyst of Fisher-Tropsch synthesis in slurry bed |
-
2005
- 2005-06-21 CN CNB2005100269682A patent/CN100404137C/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106311361A (en) * | 2015-06-24 | 2017-01-11 | 神华集团有限责任公司 | System and method for activation and online renewing of catalyst |
| 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 |
| US11629293B2 (en) | 2020-03-10 | 2023-04-18 | Yankuang Energy R&D Co., Ltd., Shanghai | System for producing hydrocarbons by high-temperature Fischer-Tropsch synthesis |
| WO2023092377A1 (en) * | 2021-11-25 | 2023-06-01 | 国家能源投资集团有限责任公司 | Method and device for continuous operation of fischer-tropsch synthesis catalyst |
| CN114345340A (en) * | 2022-01-08 | 2022-04-15 | 安庆市长虹化工有限公司 | Preparation process and working system of carrier copper nanotube dehydrogenation catalyst |
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| CN100404137C (en) | 2008-07-23 |
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Application publication date: 20060809 Assignee: Shaanxi Weilai Energy Chemical Co., Ltd. Assignor: Shanghai Yankuang Energy Source Science and Technology Research Development Co. Contract record no.: 2017310000029 Denomination of invention: Industrial reduction method of particle iron-base fischer-tropsch synthesis catalyst Granted publication date: 20080723 License type: Common License Record date: 20170626 |
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