CN202638399U - Reactor for modulating Fischer-Tropsch synthetic product distribution - Google Patents
Reactor for modulating Fischer-Tropsch synthetic product distribution Download PDFInfo
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- CN202638399U CN202638399U CN 201220116865 CN201220116865U CN202638399U CN 202638399 U CN202638399 U CN 202638399U CN 201220116865 CN201220116865 CN 201220116865 CN 201220116865 U CN201220116865 U CN 201220116865U CN 202638399 U CN202638399 U CN 202638399U
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Abstract
A reactor for modulating Fischer-Tropsch synthetic product distribution belongs to the technical field of hypergravity reactors. The reactor comprises a sealed reactor shell, a rotor fixed with catalyst bed layers, a rotating shaft, an end cover, a reactant inlet and a product outlet. The rotor of a rotating packed bed catalytic reactor is provided with multiple concentric ring-type catalyst bed layers therein; an interlayer heat transfer section is arranged between every two catalyst bed layers; the interlayer heat transfer section is a concentric ring formed by a plurality of separated casing pipes or heat pipes surrounding the center of the rotor; the end cover is provided with a heat transfer medium inlet and outlet device; and the outer edge of the rotor is provided with blades. The rotating packed bed catalytic reactor changes the variety and amount of catalysts and the inner structure and hypergravity level of the hypergravity reactor to synthesize products with specific component distribution with high selectivity. The hypergravity rotating packed bed catalytic reactor with a novel structure of the utility model has the advantages of orientated production of the target products, good heat and mass transfer performances, long service life of catalysts, etc.
Description
Technical field
The utility model relates to the reactor that a kind of modulation Fischer-Tropsch synthetic distributes, and specifically, relates to a kind of RPB catalytic reactor that is made of multi-layer rotor and heat exchanging segment the concentric ring type catalyst layer that has, and belongs to the supergravity reactor technical field.
Background technology
Contain hydrocarbon raw material and produce synthesis gas (CO, CO so that natural gas, pitch, coal, living beings etc. are various
2And H
2Mist), again take synthesis gas as raw material by the synthetic liquefied hydrocarbon of producing of Fischer-Tropsch, be a good oil replacement technology.Fischer-Tropsch synthesizes (Fischer-Tropsch process), claims again F-T synthetic, is synthetic take paraffin hydrocarbon as main liquid fuel technical process under catalyst and felicity condition take synthesis gas as raw material.Existing more than 80 years of Fischer-Tropsch synthesis is historical, and what have now that fairly large Fischer-Tropsch synthesizes production capacity has Sasol, PetroSA, Shell and an Oryx company etc.In recent years, along with petroleum resources exhaust gradually and world wide in constantly soaring to new forms of energy and resource requirement, the approach by Fischer-Tropsch synthesis prepare liquid fuel or high valuable chemicals has obtained extensive approval.
The Fischer-Tropsch synthesis device of having reported has various ways, comprises fixed bed, fluid bed and slurry attitude bed etc.Adopt fixed bed reactors to carry out fischer-tropsch reaction and before half a century, just realized industrialization, but removing with the inactivation problem of catalyst of reaction heat is particularly outstanding.Because Fischer-Tropsch synthesis is strong exothermal reaction, if reaction heat is not in time removed, catalyst just hot localised points occurs easily, causes the inactivation of catalyst and the elective reduction of long chain alkane product, the moment temperature runaway phenomenon that can occur reactor in the serious situation, the device parking maintenance of having to.Adopting paste state bed reactor is to solve Fischer-Tropsch synthesis to move one of effective means of heat problem, especially all the more so concerning large-scale device, but the use of paste state bed reactor also brings new problem.In paste state bed reactor, tiny catalyst granules and liquid hydrocarbon product mix, and their effective separation difficulty is in fact and not second to other technical barriers that faces, and this is the main problem that such reactor faces.In addition, people know little to the three-phase fluid mechanical behavior in the slurry attitude bed, and this brings certain difficulty also for the amplification of paste state bed reactor.
The high-gravity technology that grew up in 1976, its core are high gravity rotating packed bed.Packed bed inside is a High Rotation Speed rotor of filling filler, and its centrifugal acceleration is the tens of to thousands of times of acceleration of gravity.The high-gravity rotating bed centrifugal force field of utilizing is simulated super gravity field, and its core is the very big reinforcement to transmittance process and micro mixing.Along with developing rapidly of high-gravity technology, (see for details Chinese patent 92102061,95105344.2,200710120712.7,200810103231 etc.) obtained application to high-gravity technology in fields such as oil-field flooding deoxidation, ultramicro powder preparation, polymer devolatilization, collecting carbonic anhydride, rectifying.But existing high gravity rotating packed bed still can not be controlled reaction condition accurately carrying out Fischer-Tropsch when synthetic, can not further remove such as reaction heat, can make inhomogeneous, the inaccuracy of reaction condition, can not regulate and control well the distribution of product; The time of reactant in catalyst is long, affects catalytic activity etc.
The utility model content
The utility model provides a kind of new structure RPB catalytic reactor for the distribution of modulation Fischer-Tropsch synthetic, can solve the exothermic heat of reaction problem, thereby accurate controlled condition can be regulated and control the distribution of product well.
For achieving the above object, the technical solution adopted in the utility model is as follows.
A kind of high gravity rotating packed bed catalytic reactor for the distribution of modulation Fischer-Tropsch synthetic, comprise airtight reactor shell, be fixed with the rotor, rotating shaft, end cap, the import of reactant, the outlet of product of beds, it is characterized in that, be furnished with multilayer concentric ring type beds in the catalytic reactor rotor, seal between catalyst layer and the end cap, every two-layer catalyst bed interlayer is distributed with the interlayer heat exchanging segment of concentric ring type, can in time shift out reaction heat; Between be separated with the interlayer heat exchanging segment two-layer beds communicate, reactant is continuously by a plurality of beds, thereby make every layer of catalyst can both touch reaction mass, the import of reactant is positioned at the center of rotor, have the product outlet on the housing, the rotor outer rim is provided with blade, is used for unreacted gas material and product are transported to gas outlet tube, avoids the return catalizer layer.The interlayer heat exchanging segment is a plurality of sleeve pipes (41 among Fig. 1) or the donut that forms around rotor center of heat pipe separately, and end cap is provided with heat transferring medium import and outlet device, thereby realizes that heat transferring medium is to the temperature control of sleeve pipe or heat pipe.
Above-mentioned beds divides 2 layers or multilayer to be fixed on the rotor, between every two-layer ring thermosphere the interlayer heat exchanging segment is arranged all, and heat exchanging segment distributes along the radial concentric of rotor; The outer surface of heat pipe is perpendicular to axial direction to be furnished with heat exchange fin (see Fig. 4 43), and sleeve pipe is preferred finned sleeve pipe (see Fig. 3 42) also.
The concentric ring type beds is to be fixed on epitrochanterian concentric ring type silk screen layer or the immobilized concentric ring Integral-structure type filler that the catalyst activity component is arranged that is coated with catalyst granules.
The preparation material of heat pipe or sleeve pipe is: steel, monel, the Ying Kenaier alloy, the alloy of aluminium, titanium, nickel, copper, brass or any aforementioned metal, macromolecular material, pottery, glass comprises the composite of macromolecular material and glass fibre, quartz, silicon, a kind of, two or more combination in the above-mentioned substance.
The preparation material of rotor is: the alloy of steel, monel, Ying Kenaier alloy, aluminium, titanium, nickel, copper, brass or any aforementioned metal; Two or more combination of macromolecular material, pottery, glass, the composite that comprises macromolecular material and glass fibre, quartz, silicon or its.
When above-mentioned interlayer heat exchanging segment is sleeve pipe, the import of heat transferring medium and outlet device are to be parallel to two blocks of plectanes concentric with rotor that end cap is stacking, two plectanes and the end cap interval that has living space each other, the periphery of two plectanes is fixed and is sealed on the end cap, be fixed on the end cap to the outermost layer vertical seal of sleeve pipe, the inner tube port of sleeve pipe passes near the plectane of end cap and sealing and is fixed on the plectane, and offer the heat transferring medium inlet tube at this plectane, the heat transferring medium inlet tube passes outmost plectane, outmost plectane is provided with the heat transferring medium outlet, and heat transferring medium removes heat by sleeve pipe.
When above-mentioned interlayer heat exchanging segment is heat pipe, the import of heat transferring medium and outlet device are to be parallel to end cap, to be sealingly fastened in plectane end cap, concentric with rotor all around, two ends at the diameter of this plectane are provided with heat transferring medium inlet tube and outlet, the heat pipe sealing is fixed on the end cap, one end is positioned at the interlayer heat exchanging segment, the other end is between end cap and plectane, and heat transferring medium shifts out heat by heat pipe between end cap and the plectane.
Supergravity reactor of the present utility model comprises horizontal with vertical.Horizontal supergravity reactor, the product outlet is located at the tangential direction of rotor.Vertical rotating packed bed catalytic reactor the sealing housing and rotor between be provided with lower leaf-pushing plate, products export is arranged on the position of rotating shaft on the housing, and be provided with the axial flow element in the exit, so that unreacted gas material and product in time leave reactor.
Supergravity reactor of the present utility model is preferred: the horizontal supergravity reactor of sleeve heat exchange (seeing Fig. 1), the horizontal supergravity reactor of finned sleeve heat exchange (Fig. 3), the horizontal supergravity reactor of heat pipe heat exchanging (Fig. 4), the vertical supergravity reactor of heat pipe heat exchanging (Fig. 5).
Product and intermediate product overstand on catalyst is one of reason of catalyst carbon deposition, and carbon distribution is one of major reason of fischer-tropsch reaction catalysqt deactivation.Therefore, reduce product and suppressible catalysqt deactivation of the time of staying of intermediate product on catalyst, the service life of extending catalyst.Because the RPB catalytic reactor can be strengthened mass transfer and course of reaction, the above-mentioned conversion reaction of in the RPB catalytic reactor, carrying out, can strengthen the mass transfer between product and the catalyst, reduce the impact of product diffusion couple catalytic reaction process, arrange gas outlet tube by the tangential direction at horizontal rotary packed bed catalytic reactor rotor, in vertical rotating packed bed catalytic reactor gas outlet tube, the axial flow element is set, make the reactant reaction environment that speeds away, impel reactant to move to the product direction, thereby overcome the shortcoming of popular response device, reach and improve the catalyst utilization ratio, improve catalyst selectivity, reduce accessory substance and generate, reduce the effect of energy consumption.Simultaneously, because the reinforcement of diabatic process is removed rapidly reaction heat, make more for a long time reposefully operation of catalytic reaction.
Because Fischer-Tropsch synthesis is strong exothermal reaction, catalyst can be because of the overheated activity decay that causes, the simultaneous reactions heat of therefore carrying out in reaction must in time shift out beds, the heat exchanging segment of multipiece rotor of the present utility model can shift out beds with reaction heat effectively, according to the differential responses process conditions, but the heat exchange mode that choice for use is different and heat transferring medium (heat transferring medium of use comprises gas, liquid), thereby the temperature that ensures beds is accurately controlled, thereby reaches the distribution of control product.
The application of the reactor that above-mentioned modulation Fischer-Tropsch synthetic distributes, the catalyst of Fischer-Tropsch synthesis is installed in the beds of rotor, beds is in the High Rotation Speed state all the time in the course of reaction, heat transferring medium adopts liquid or gas, and the import by heat transferring medium enters, after the heat exchange, get rid of by the heat transferring medium outlet, reaction mass is entered by reaction-ure inlet, and by beds and the interlayer heat exchanging segment of High Rotation Speed, the product of generation is discharged by the product outlet; Reaction mass is coal based synthetic gas, natural gas base synthesis gas, coal bed gas base synthesis gas or Biomass Syngas, and it consists of the CO+CO of various ratios
2+ H
2, CO+H
2, CO
2+ H
2The hypergravity level of RPB catalytic reactor is 2-400g; Reaction temperature is 180 ℃-500 ℃, and reaction pressure is 1-100atm, and gas space velocity is 100-100000h
-1
Supergravity reactor for Fischer-Tropsch synthesis of the present utility model has following advantage:
The inner structure of kind, consumption and RPB catalytic reactor by changing catalyst and the temperature of hypergravity level and reaction etc., can optionally synthesize specific products, the catalyst of fischer-tropsch reaction comprises the Co base of the whole bag of tricks preparation, the catalyst such as Ru is basic and Fe is basic.Exothermic heat of reaction is taken rapidly out of conversion zone, therefore is easy to control reaction temperature, and be applicable to Fischer-Tropsch synthesis and regulate and control reactant distribution, the mass transfer of Fischer-Tropsch synthesis, good heat-transfer, catalyst activity and selectivity of product are stable, and catalyst life is long.
Description of drawings
Fig. 1 is the horizontal supergravity reactor schematic diagram of sleeve heat exchange;
Fig. 2 is the side view of horizontal supergravity reactor;
Fig. 3 is the horizontal supergravity reactor schematic diagram of finned sleeve heat exchange;
Fig. 4 is the horizontal supergravity reactor schematic diagram of heat pipe heat exchanging;
Fig. 5 is the vertical supergravity reactor schematic diagram of heat pipe heat exchanging;
1 end cap, 2 heat transferring medium imports, 3 reaction-ure inlets, 41 sleeve-type heat exchanging pipes, the finned sleeve-type heat exchanging pipe of 42 outer tubes, 43 finned heat pipe type heat exchanger pipes, the outlet of 5 heat transferring mediums, 6 interior sealings, 7 beds, 8 blades, 9 housings, 10 sealings, 11 rotating shafts, the outlet of 12 products, 13 times leaf-pushing plates, 14 axial flow elements.
The specific embodiment
Be used for the high gravity rotating packed bed catalytic reactor that the modulation Fischer-Tropsch synthetic distributes, comprise airtight reactor shell 9 (and sealing by sealing 10 between the rotating shaft), the rotor that is fixed with beds 7, rotating shaft 11, end cap 1, the import 3 of reactant, the outlet 12 of product, it is characterized in that, be furnished with multilayer concentric ring type beds in the catalytic reactor rotor, seal by interior sealing 6 between catalyst layer and the end cap, every two-layer catalyst bed interlayer is distributed with the interlayer heat exchanging segment of concentric ring type, can in time shift out reaction heat; Between be separated with the interlayer heat exchanging segment two-layer beds communicate, thereby being flowed, reactant continues reaction between the multi-layer catalyst bed, the import of reactant is positioned at the center of rotor, have the product outlet on the housing, the rotor outer rim is provided with blade 8, be used for unreacted gas material and product are transported to gas outlet tube, avoid the return catalizer layer.The interlayer heat exchanging segment is a plurality of sleeve pipes or the donut that forms around rotor center of heat pipe separately, and end cap is provided with heat transferring medium import 2 and outlet 5 devices, thereby realizes that heat transferring medium is to the temperature control of sleeve pipe or heat pipe.
The RPB catalytic reactor is horizontal or vertical, and the horizontal reactor gas outlet tube is arranged on the housing along the tangential direction of rotor; Vertical rotating packed bed catalytic reactor is provided with lower leaf-pushing plate between the housing that seals and rotor, see 13 of Fig. 5, is provided with the axial flow element in the gas outlet tube, sees 14 of Fig. 5.
Fischer-tropsch synthetic catalyst is installed on the multipiece rotor of supergravity reactor, and beds is in the High Rotation Speed state all the time in the course of reaction.Synthesis gas is entered by the entrance of supergravity reactor, by the beds of High Rotation Speed.The product that generates is discharged by the supergravity reactor outlet, and measures through gas chromatographic analysis.The reaction heat of emitting in course of reaction can shift out from reactor by the heat exchanger tube of catalyst bed interlayer.Different according to catalyst and synthesis gas conversion ratio can adopt respectively heat pipe, sleeve pipe and finned sleeve pipe to carry out heat exchange, and heat transferring medium can use liquid or gas.
Utilize supergravity reactor to carry out Fischer-Tropsch paraffin reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Co/SiO
2Fischer-tropsch catalysts is put into the mesh-supported part, is fixed on the rotor of supergravity reactor, adopts the horizontal supergravity reactor of sleeve heat exchange, sees Fig. 1, and side view is seen Fig. 2, and sleeve pipe is Steel material, and heat transferring medium is air, and the flow velocity of heat transferring medium is 1 liter/min of clock.
The process conditions of reaction are as follows:
Synthesis gas air speed: 1600h
-1, reaction temperature: 210 ℃, reaction pressure: 2.2MPa
Beds rotating speed: 10rpm, beds hypergravity level: 3g
Supergravity reactor carries out the synthetic paraffin reaction result processed of Fischer-Tropsch:
Utilize supergravity reactor to carry out Fischer-Tropsch paraffin reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Ru/SiO
2Fischer-tropsch catalysts is put into the mesh-supported part, is fixed on the rotor of supergravity reactor, adopts the vertical supergravity reactor of finned sleeve heat exchange, sees Fig. 3.Sleeve pipe is aluminum, and heat transferring medium is that air changes, and the flow velocity of thermal medium is 2 liter/mins of clocks.
The process conditions of reaction are as follows:
Synthesis gas air speed: 5000h
-1, reaction temperature: 190 ℃, reaction pressure: 6.0MPa
Beds rotating speed: 80rpm, beds hypergravity level: 10g
Supergravity reactor carries out the synthetic paraffin reaction result processed of Fischer-Tropsch:
Utilize supergravity reactor to carry out Fischer-Tropsch paraffin reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/1.The iron-base fischer-tropsch catalyst is put into the mesh-supported part, be fixed on the rotor of supergravity reactor, adopt the vertical supergravity reactor of heat pipe heat exchanging, see Fig. 5.Heat pipe is that Steel material changes, and thermal medium is conduction oil, and the flow velocity of heat transferring medium is 1 liter/min of clock.
The process conditions of reaction are as follows:
Synthesis gas air speed: 2000h
-1, reaction temperature: 280 ℃, reaction pressure: 3.0MPa
Beds rotating speed: 100rpm, beds hypergravity level: 20g
Supergravity reactor carries out the synthetic paraffin reaction result processed of Fischer-Tropsch:
Embodiment 4
Utilize supergravity reactor to carry out Fischer-Tropsch diesel oil reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Ru/SiO
2Fischer-tropsch catalysts is put into the mesh-supported part, is fixed on the rotor of supergravity reactor.Adopt the vertical supergravity reactor of heat pipe heat exchanging, see Fig. 5.Heat pipe is Steel material, and heat transferring medium is air, and the flow velocity of heat transferring medium is 1 liter/min of clock.
The process conditions of reaction are as follows:
Synthesis gas air speed: 600h
-1, reaction temperature: 190 ℃, reaction pressure: 5MPa
Beds rotating speed: 500rpm, beds hypergravity level: 60g
Supergravity reactor carries out the synthetic diesel oil reaction result processed of Fischer-Tropsch:
Utilize supergravity reactor to carry out Fischer-Tropsch gasoline reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Ru/SiO
2Fischer-tropsch catalysts is put into the mesh-supported part, is fixed on the rotor of supergravity reactor.Adopt the vertical supergravity reactor of heat pipe heat exchanging, see Fig. 5.Heat pipe is Steel material, and heat transferring medium is air, and the flow velocity of heat transferring medium is 1 liter/min of clock.
The process conditions of reaction are as follows:
Synthesis gas air speed: 500h
-1, reaction temperature: 210 ℃, reaction pressure: 0.5MPa
Beds rotating speed: 2500rpm, beds hypergravity level: 150g
Supergravity reactor carries out the synthetic gasoline reaction result processed of Fischer-Tropsch:
Utilize supergravity reactor to carry out the synthetic reaction for preparing light olefins of Fischer-Tropsch.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Ru/SiO
2Fischer-tropsch catalysts is put on the rotor that the mesh-supported part is fixed in supergravity reactor.Adopt the vertical supergravity reactor of heat pipe heat exchanging, see Fig. 5.Heat pipe is copper product, and heat transferring medium is air, and the flow velocity of heat transferring medium is 1 liter/min of clock.
The process conditions of reaction are as follows:
Synthesis gas air speed: 7500h
-1, reaction temperature: 250 ℃, reaction pressure: 2.5MPa
Beds rotating speed: 5000rpm, beds hypergravity level: 250g
Supergravity reactor carries out the synthetic reaction for preparing light olefins result of Fischer-Tropsch:
Utilize supergravity reactor to carry out Fischer-Tropsch alkynes reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/2.With Co/SiO
2Fischer-tropsch catalysts is put into the mesh-supported part, is fixed on the rotor of supergravity reactor, adopts the vertical supergravity reactor of heat pipe heat exchanging, sees Fig. 5.Heat pipe is copper product, and heat transferring medium is air, and the flow velocity of heat transferring medium is 3 liter/mins of clocks.
The process conditions of reaction are as follows:
Synthesis gas air speed: 3000h
-1, reaction temperature: 350 ℃, reaction pressure: 0.6MPa
Beds rotating speed: 8500rpm, beds hypergravity level: 400g
Supergravity reactor carries out the synthetic alkynes reaction result processed of Fischer-Tropsch:
Utilize supergravity reactor to carry out Fischer-Tropsch alkynes reaction synthetic processed.Synthesis gas is CO+H
2Gaseous mixture, CO/H
2=1/1.The iron-base fischer-tropsch catalyst is put into the mesh-supported part, be fixed on the rotor of supergravity reactor.Adopt the vertical supergravity reactor of heat pipe heat exchanging, see Fig. 5.Heat pipe is that the copper product heat transferring medium is that the flow velocity of air heat-exchange medium is 2 liter/mins of clocks
The process conditions of reaction are as follows:
Synthesis gas air speed: 1000h
-1, reaction temperature: 210 ℃, reaction pressure: 2.0MPa
Beds hypergravity level: 350g
Supergravity reactor carries out the synthetic alkynes reaction result processed of Fischer-Tropsch:
Claims (7)
1. the reactor that distributes of a modulation Fischer-Tropsch synthetic, this reactor is the high gravity rotating packed bed catalytic reactor, comprise airtight reactor shell, be fixed with the rotor, rotating shaft, end cap, the import of reactant, the outlet of product of beds, it is characterized in that, be furnished with multilayer concentric ring type beds in the catalytic reactor rotor, seal between catalyst layer and the end cap, every two-layer catalyst bed interlayer is distributed with the interlayer heat exchanging segment of concentric ring type; Between be separated with the interlayer heat exchanging segment two-layer beds communicate, reactant is continuously by a plurality of beds, thereby make every layer of catalyst can both touch reaction mass, the import of reactant is positioned at the center of rotor, have the product outlet on the housing, the rotor outer rim is provided with blade, be used for unreacted gas material and product are transported to gas outlet tube, the interlayer heat exchanging segment is a plurality of sleeve pipes or the donut that forms around rotor center of heat pipe separately, and end cap is provided with heat transferring medium import and outlet device.
2. according to reactor claimed in claim 1, it is characterized in that beds divides 2 layers or multilayer to be fixed on the rotor, between every two-layer ring thermosphere the interlayer heat exchanging segment is arranged all, heat exchanging segment distributes along the radial concentric of rotor; The outer surface of the heat pipe heat exchange fin that is furnished with perpendicular to axial direction, sleeve pipe is finned sleeve pipe.
3. according to reactor claimed in claim 1, it is characterized in that the concentric ring type beds is to be fixed on epitrochanterian concentric ring type silk screen layer or the immobilized concentric ring Integral-structure type filler that the catalyst activity component is arranged that is coated with catalyst granules.
4. according to reactor claimed in claim 1, it is characterized in that, when the interlayer heat exchanging segment is sleeve pipe, the import of heat transferring medium and outlet device are to be parallel to two blocks of plectanes concentric with rotor that end cap is stacking, two plectanes and the end cap interval that has living space each other, the periphery of two plectanes is fixed and is sealed on the end cap, be fixed on the end cap to the outermost layer vertical seal of sleeve pipe, the inner tube port of sleeve pipe passes near the plectane of end cap and sealing and is fixed on the plectane, and offer the heat transferring medium inlet tube at this plectane, the heat transferring medium inlet tube passes outmost plectane, and outmost plectane is provided with the heat transferring medium outlet, and heat transferring medium removes heat by sleeve pipe;
When the interlayer heat exchanging segment is heat pipe, the import of heat transferring medium and outlet device are to be parallel to end cap, to be sealingly fastened in plectane end cap, concentric with rotor all around, two ends at the diameter of this plectane are provided with heat transferring medium inlet tube and outlet, the heat pipe sealing is fixed on the end cap, one end is positioned at the interlayer heat exchanging segment, the other end is between end cap and plectane, and heat transferring medium shifts out heat by heat pipe between end cap and the plectane.
5. according to reactor claimed in claim 1, it is characterized in that for horizontal, the product outlet is located at the tangential direction of rotor.
6. according to reactor claimed in claim 1, it is characterized in that, for vertical, vertical rotating packed bed catalytic reactor the sealing housing and rotor between be provided with lower leaf-pushing plate, products export is arranged on the position of rotating shaft on the housing, and is provided with the axial flow element in the exit.
7. according to the arbitrary described reactor of claim 1-6, it is characterized in that, be the horizontal supergravity reactor of sleeve heat exchange, the horizontal supergravity reactor of finned sleeve heat exchange, the horizontal supergravity reactor of heat pipe heat exchanging or the vertical supergravity reactor of heat pipe heat exchanging.
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| CN 201220116865 CN202638399U (en) | 2012-03-26 | 2012-03-26 | Reactor for modulating Fischer-Tropsch synthetic product distribution |
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|---|---|---|---|
| CN 201220116865 CN202638399U (en) | 2012-03-26 | 2012-03-26 | Reactor for modulating Fischer-Tropsch synthetic product distribution |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102626600A (en) * | 2012-03-26 | 2012-08-08 | 北京化工大学 | Reactor for distribution modulation of Fischer-Tropsch synthesis product and application thereof |
| CN104549100A (en) * | 2013-10-16 | 2015-04-29 | 北京化工大学 | Novel passive super-gravity rotary bed device |
| CN104741063A (en) * | 2013-12-27 | 2015-07-01 | 超重力有限公司 | Rotary packed bed device |
| CN105080446A (en) * | 2014-04-18 | 2015-11-25 | 北京化工大学 | Multi-stage material feeding supergravity liquid-liquid reactor apparatus and applications thereof |
| CN113368793A (en) * | 2020-02-25 | 2021-09-10 | 北京化工大学 | Rotating equipment for accurate temperature control of thermosensitive substance and application method thereof |
-
2012
- 2012-03-26 CN CN 201220116865 patent/CN202638399U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102626600A (en) * | 2012-03-26 | 2012-08-08 | 北京化工大学 | Reactor for distribution modulation of Fischer-Tropsch synthesis product and application thereof |
| CN102626600B (en) * | 2012-03-26 | 2014-05-21 | 北京化工大学 | Reactor for distribution modulation of Fischer-Tropsch synthesis product and application thereof |
| CN104549100A (en) * | 2013-10-16 | 2015-04-29 | 北京化工大学 | Novel passive super-gravity rotary bed device |
| CN104741063A (en) * | 2013-12-27 | 2015-07-01 | 超重力有限公司 | Rotary packed bed device |
| CN105080446A (en) * | 2014-04-18 | 2015-11-25 | 北京化工大学 | Multi-stage material feeding supergravity liquid-liquid reactor apparatus and applications thereof |
| CN105080446B (en) * | 2014-04-18 | 2017-08-15 | 北京化工大学 | A kind of multistage charging hypergravity L-L reactor device and its application |
| CN113368793A (en) * | 2020-02-25 | 2021-09-10 | 北京化工大学 | Rotating equipment for accurate temperature control of thermosensitive substance and application method thereof |
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