CN202478905U - Slurry bubble column reactor - Google Patents
Slurry bubble column reactor Download PDFInfo
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- CN202478905U CN202478905U CN2012200421967U CN201220042196U CN202478905U CN 202478905 U CN202478905 U CN 202478905U CN 2012200421967 U CN2012200421967 U CN 2012200421967U CN 201220042196 U CN201220042196 U CN 201220042196U CN 202478905 U CN202478905 U CN 202478905U
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Abstract
The utility model discloses a slurry bubble column reactor to solve the problem that uneven synthesis gas distribution is easy to cause in existing slurry bubble column reactors. The slurry bubble column reactor is provided with a reactor casing (1), a partition board (8) is arranged on the upper portion of the reactor casing, a distribution board (32) is arranged on the lower portion, and a bubble cap distributor (31) is arranged on the distribution board. A heat exchange tube (5), a liquid solid separator (4), gas liquid cyclone (7) and a circulation cup (6) are arranged in the reactor casing. An air inlet pipe (10) is arranged on a bottom sealing head of the reactor casing, and an air outlet pipe (11) is arranged on a top sealing head. A pre-distributor (2) is arranged below the distribution board, and is a rotary panel protruding upward and with a shaft axis of the reactor casing serving as a rotating shaft, and a plurality of holes are opened evenly on the pre-distributor. The bottom edge of the pre-distributor is connected to the bottom sealing head of the reactor casing. The slurry bubble column reactor is mainly used for the Fischer Tropsch synthesis process.
Description
Technical field
The utility model belongs to the chemical industry equipment field, relates to a kind of gas-liquid-solid three-phase paste state bed reactor that is used for fischer-tropsch synthesis process.
Background technology
Paste state bed reactor is the key equipment in the fischer-tropsch synthesis process, and wherein liquid is that continuous phase, gas and solid are decentralized photo.Paste state bed reactor utilizes the power source of synthesis gas as the reaction mixing, catalyst is suspended in the liquid phase reacts; Owing to do not have mechanical agitation, thereby can under high pressure not have the operation of leakage.Again because paste state bed reactor has high liquid storage amount; For the very big reaction engineering of reaction heat; Can remove effectively heat of reaction, realization response device isothermal operation, avoid occurring the bed focus, prolong life of catalyst, thereby guarantee the normal operation of paste state bed reactor.
The patent of relevant paste state bed reactor is more.Chinese patent CN201735386U discloses a kind of synthetic paste state bed reactor of Fischer-Tropsch that is used for, and is provided with reactor shell; Reactor shell top is provided with dividing plate, and the bottom is provided with distribution grid, and the top of distribution grid is provided with heat exchanger tube.The circulation cup that is axially arranged with gas-liquid cyclone separator and top band extension mouth along reactor shell.Each gas-liquid cyclone separator all with the coaxial corresponding layout of circulation cup, the dipleg of gas-liquid cyclone separator bottom stretches in the extension mouth at circulation cup top of correspondence.The escape pipe of gas-liquid cyclone separator passes dividing plate, and the escape pipe top exit is positioned at the top of dividing plate.The outlet at bottom of circulation cup is positioned at the top of distribution grid; Be provided with the bubble cap distributor on the distribution grid equably, the below of distribution grid is a gas-phase space.The bottom bulkhead of reactor shell is provided with air inlet pipe, and the top end socket of reactor shell is provided with gas outlet tube.In the operating process, the gas-phase space of synthesis gas below air inlet pipe gets into distribution grid, the form with bubble after the bubble cap distributor distributes gets in the slurry attitude bed.The problem that exists is because synthesis gas only once distributes through the bubble cap distributor, to cause its skewness easily.Along with the continuous expansion of paste state bed reactor industrially scalable, its diameter increases rapidly, has reached 5～10m at present; Guaranteeing the uniformity that synthesis gas distributes, is crucial.
Summary of the invention
The purpose of the utility model provides a kind of paste state bed reactor, to solve the existing synthesis gas problem pockety that causes easily of existing paste state bed reactor.
For addressing the above problem, the technical scheme that the utility model adopts is: a kind of paste state bed reactor is provided with reactor shell; The top of reactor shell is provided with dividing plate, and the bottom is provided with distribution grid, and distribution grid is provided with the bubble cap distributor; The top of distribution grid is provided with heat exchanger tube; Along reactor shell be axially arranged with gas-liquid cyclone separator and circulation cup, the bottom bulkhead of reactor shell is provided with air inlet pipe, the top end socket of reactor shell is provided with gas outlet tube; It is characterized in that: paste state bed reactor is provided with liquid-solid separator; Below distribution grid, be provided with pre-distributor, pre-distributor be raise up, be the surface of revolution shape plate of gyroaxis with the axial line of reactor shell, be provided with perforate on it equably; The bottom margin of pre-distributor is connected on the bottom bulkhead of reactor shell, and air inlet pipe is connected with the space between the bottom bulkhead of pre-distributor and reactor shell.
Adopt the utility model; Has following beneficial effect: in the operating process; Synthesis gas gets into the space between pre-distributor and the reactor shell bottom bulkhead through air inlet pipe; Flow into the space between distribution grid-pre-distributor-reactor shell bottom bulkhead through the perforate on the pre-distributor, carried out once presorting cloth.Presort the uniformity that the synthesis gas behind the cloth distributes and be improved, can get into each bubble cap distributor with flow with the pressure of basically identical and distribute again, thereby can distribute relatively more evenly.The uniformity that the said synthesis gas of the utility model distributes is meant the uniformity that synthesis gas distributes on the paste state bed reactor cross section.
Below in conjunction with the accompanying drawing and the specific embodiment the utility model is done further detailed explanation.The accompanying drawing and the specific embodiment do not limit the scope of the utility model requirement protection.
Description of drawings
Fig. 1 is the structural representation of the utility model paste state bed reactor.
Fig. 2 is the partial enlarged drawing of gas-liquid cyclone separator shown in Figure 1.
Fig. 3 is the A-A cutaway view among Fig. 2.
Fig. 4 is the B-B cutaway view among Fig. 3.
Fig. 5 is that outer surface is provided with the heat exchanger tube of aciculiform fin or the cross-sectional view of circulation cup.
Among Fig. 1 to Fig. 5, same reference numerals is represented identical technical characterictic.
The specific embodiment
Referring to Fig. 1, the paste state bed reactor of the utility model is provided with reactor shell 1.The top of reactor shell 1 is provided with dividing plate 8, and the bottom is provided with distribution grid 32.Be provided with a plurality of bubble cap distributors 31 on the distribution grid 32 equably, the top of distribution grid 32 is provided with heat exchanger tube 5.Along the circulation cup 6 of a plurality of gas-liquid cyclone separators 7 of being axially arranged with of reactor shell 1 and top band extension mouth, the bottom of circulation cup 6 is positioned at the top of distribution grid 32.Each gas-liquid cyclone separator 7 all with circulation cup 6 coaxial corresponding layouts, the dipleg 73 of gas-liquid cyclone separator 7 bottoms stretches in the extension mouth at circulation cup 6 tops of correspondence.The bottom bulkhead of reactor shell 1 is provided with air inlet pipe 10, and the top end socket of reactor shell 1 is provided with gas outlet tube 11.Above characteristic, basic identical with the described paste state bed reactor of CN201735386U.Wherein, heat exchanger tube 5 can use winding type multipass heat exchanger tube or helical disk tubular type heat exchanger tube (of CN1233451C), and one section or two sections are set.
The paste state bed reactor of the utility model is provided with liquid-solid separator 4; Liquid-solid separator 4 is generally metal filtration pipe or ceramic filter tube, preferably can carry out the metal filtration pipe that blowback is cleaned.The utility model can use CN1233451C, the described liquid-solid separation device of CN101396647B.When heat exchanger tube 5 was provided with one section, liquid-solid separator 4 was located at the top (as shown in Figure 1) of this section heat exchanger tube 5.When heat exchanger tube was provided with two sections, liquid-solid separator was located at the position (figure slightly) between these two sections heat exchanger tubes.
The paste state bed reactor of the utility model is provided with pre-distributor 2 below distribution grid 32.Pre-distributor 2 for raise up, be the surface of revolution shape plate of gyroaxis with the axial line of reactor shell 1, be provided with a plurality of perforates (being generally circular port) on it equably.The bottom margin of pre-distributor 2 is connected on the bottom bulkhead of reactor shell 1, and air inlet pipe 10 is connected with the space between the bottom bulkhead of pre-distributor 2 and reactor shell 1.
The bus of pre-distributor 2 is generally one section circular arc or one section elliptic arc.
Existing paste state bed reactor, heat exchanger tube generally is light pipe with the circulation cup, does not have the bubble breaking function, helps the coalescence of bubble in uphill process on the contrary; The heat transfer intensity of light pipe heat exchanger tube is generally lower in addition.CN201684588U proposes, and heat exchanger tube adopts axial kerve pipe to enlarge heat exchange area, and still this axial kerve pipe does not have the effect of bubble crushing, raising slurries void fraction and gas-liquid mass-transfer efficiency.For addressing the above problem, the utility model can be provided with aciculiform fin 9 on the outer surface of heat exchanger tube 5 and circulation cup 6, like Fig. 1, shown in Figure 5; Pipe among Fig. 5 is represented heat exchanger tube 5 or circulation cup 6.Aciculiform fin 9 generally is to be welded on the outer surface of heat exchanger tube 5 and circulation cup 6.When bubble rose in slurry attitude bed, aciculiform fin 9 can prevent its coalescence on the outer surface of heat exchanger tube 5 and circulation cup 6 with its fragmentation, thereby can improve void fraction, the raising gas-liquid mass transfer efficient of slurries.Because the receptor area of aciculiform fin 9 on paste state bed reactor is axial is less, catalyst can not gather on aciculiform fin 9, is favourable for guard catalyst.In addition, on heat exchanger tube 5 outer surfaces aciculiform fin 9 is set, can also enlarges heat exchange area, and make the gas-liquid-solid three-phase slurry stream when the outer surface of heat exchanger tube 5, form strong turbulent flow; This all helps improving the heat transfer efficiency between the heat transferring medium in slurries and the heat exchanger tube 5.The winding type multipass heat exchanger tube of aciculiform fin 9 is set on the preferred outer surface of the utility model.
The outlet 61 of circulation cup 6 preferably is located on the sidewall of circulation cup 6 bottoms, and the bottom of circulation cup 6 is sealed with base plate.Like this, the slurries in the circulation cup 6 will can be strengthened the mixed effect of gas-liquid-solid three-phase along the Radial Flow of paste state bed reactor from exporting 61 when flowing out.Simultaneously, owing to the bottom of circulation cup 6 is sealed, the synthesis gas that gets into slurry attitude bed can only follow on the lateral of encircling cup 6 and flow.In the circulation cup 6 from exporting 61 slurries that flow out, not can with the complete reverse head-on collision of slurries of flowing on the circulation cup 6 bottom lower directions, can make the flow pattern of slurries keep stable.
The utility model can use existing gas-liquid cyclone separator, but preferably uses the gas-liquid cyclone separator of the utility model design, like Fig. 1, Fig. 2, Fig. 3 and shown in Figure 4.This gas-liquid cyclone separator 7 is coaxial to be provided with columnar cylindrical shell 71, be inverted awl section 72, dipleg 73 and the escape pipe 74 of frusto-conical face shape.The top of cylindrical shell 71 is provided with columniform sealing piece 75, radially offers the air inlet duct 76 of inclination on the sealing piece 75.Air inlet duct 76 is the radially vertical plane inclinations with respect to the sealing piece 75 of its present position.Air inlet duct 76 can be to face groove (like Fig. 3, shown in Figure 4) or helicoid groove (figure slightly) directly, offers a plurality ofly, evenly distributes along the circumferencial direction of sealing piece 75.The escape pipe 74 of gas-liquid cyclone separator 7 passes the axial line of sealing piece 75 and is fixed together with sealing piece 75; The bottom of escape pipe 74 has extension mouth, is arranged in the inner chamber of cylindrical shell 71.The top of escape pipe 74 is passed dividing plate 8 and is fixed together with dividing plate 8, in the space of the top exit of escape pipe 74 above dividing plate 8, between dividing plate 8 and the reactor shell 1 top end socket.The gas-liquid cyclone separator 7 of the utility model design in use, the gas that contains liquid carries out gas-liquid separation through the inner chambers that air inlet duct 76 directly gets into cylindrical shells 71; Advantage is that treating capacity is bigger, and separating effect can be guaranteed simultaneously.
The operating process of the utility model is following: the space of synthesis gas (main component is carbon monoxide and hydrogen) between air inlet pipe 10 entering pre-distributors 2 and reactor shell 1 bottom bulkhead; Flow into the space between the distribution grid 32-pre-distributor 2-reactor shell bottom bulkhead through the perforate on the pre-distributor 2, carried out once presorting cloth.Presort synthesis gas behind the cloth and get into each bubble cap distributor 31 and distribute again, get into afterwards in the slurry attitude bed.
Synthesis gas effect at solid catalyst in slurry attitude bed issues the reaction of intercrescence one-tenth, generates artificial oil, and emits a large amount of reaction heat (reaction heat is discharged through heat exchanger tube 5).The artificial oil that reaction generates outlet from liquid-solid separator 4 after liquid-solid separator 4 filters out solid catalyst particle is extracted out, and the extraction amount is controlled to keep normal slurry attitude bed controlling level.
Reacted synthesis tail gas (the remaining synthesis gas in reaction back and a small amount of gas that generates that reacts) carries a spot of artificial oil liquid (containing solid catalyst particle), upwards flows out slurry attitude bed.The inner chamber that the air inlet duct 76 of these synthesis tail gas on gas-liquid cyclone separator 7 sealing pieces 75 gets into gas-liquid cyclone separator 7 cylindrical shells 71 carries out gas-liquid separation, and isolated liquid gets into circulation cup 6 through dipleg 73; Isolated Purge gas is through the space that escape pipe 74 gets between dividing plate 8 and the reactor shell 1 top end socket, after gas outlet tube 11 flows out paste state bed reactor.
In the operating process, circulation cup 6 immerses in the slurries of slurry attitude bed fully, Reference numeral 12 expression slurries material levels.The slurries gas content of circulation cup 6 outsides is higher, density is lower, upwards flows.Gas content is lower, density is bigger for circulation cup 6 inner slurries (mainly being liquid and solid catalyst particle), in circulation cup 6, flows downward, and flows out from the outlet 61 of circulation cup 6 at last.
Claims (5)
1. a paste state bed reactor is provided with reactor shell (1), and the top of reactor shell (1) is provided with dividing plate (8); The bottom is provided with distribution grid (32); Distribution grid (32) is provided with bubble cap distributor (31), and the top of distribution grid (32) is provided with heat exchanger tube (5), is axially arranged with gas-liquid cyclone separator (7) and circulation cup (6) along reactor shell (1); The bottom bulkhead of reactor shell (1) is provided with air inlet pipe (10); The top end socket of reactor shell (1) is provided with gas outlet tube (11), it is characterized in that: paste state bed reactor is provided with liquid-solid separator (4), is provided with pre-distributor (2) in the below of distribution grid (32); Pre-distributor (2) for raise up, be the surface of revolution shape plate of gyroaxis with the axial line of reactor shell (1); Be provided with perforate on it equably, the bottom margin of pre-distributor (2) is connected on the bottom bulkhead of reactor shell (1), and the space between the bottom bulkhead of the same pre-distributor of air inlet pipe (10) (2) and reactor shell (1) is connected.
2. paste state bed reactor according to claim 1 is characterized in that: the bus of pre-distributor (2) is one section circular arc or one section elliptic arc.
3. paste state bed reactor according to claim 1 and 2 is characterized in that: heat exchanger tube (5) is provided with aciculiform fin (9) with the outer surface of circulation cup (6).
4. paste state bed reactor according to claim 1 and 2 is characterized in that: the outlet (61) of circulation cup (6) is located on the sidewall of circulation cup (6) bottom, the sealing of the bottom of circulation cup (6).
5. paste state bed reactor according to claim 1 and 2; It is characterized in that: gas-liquid cyclone separator (7) is provided with columnar cylindrical shell (71), is inverted awl section (72), dipleg (73) and the escape pipe (74) of frusto-conical face shape; The top of cylindrical shell (71) is provided with columniform sealing piece (75), radially offers the air inlet duct (76) of inclination on the sealing piece (75).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200421967U CN202478905U (en) | 2012-02-03 | 2012-02-03 | Slurry bubble column reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200421967U CN202478905U (en) | 2012-02-03 | 2012-02-03 | Slurry bubble column reactor |
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| Publication Number | Publication Date |
|---|---|
| CN202478905U true CN202478905U (en) | 2012-10-10 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012200421967U Expired - Lifetime CN202478905U (en) | 2012-02-03 | 2012-02-03 | Slurry bubble column reactor |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103285780A (en) * | 2012-02-24 | 2013-09-11 | 北京低碳清洁能源研究所 | Magnetic induction reactor of slurry bubble bed |
| WO2014117723A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| WO2014117725A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| CN106606998A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | Up-flow distributor and up-flow reactor |
| CN110523350A (en) * | 2018-05-24 | 2019-12-03 | 国家能源投资集团有限责任公司 | The method of paste state bed reactor and F- T synthesis |
| CN111068592A (en) * | 2019-12-30 | 2020-04-28 | 上海睿碳能源科技有限公司 | Slurry bed reactor with multi-stage perforated structure distribution plate |
| CN114053961A (en) * | 2020-08-03 | 2022-02-18 | 中国石油化工股份有限公司 | Feeding distributor and reactor |
-
2012
- 2012-02-03 CN CN2012200421967U patent/CN202478905U/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103285780A (en) * | 2012-02-24 | 2013-09-11 | 北京低碳清洁能源研究所 | Magnetic induction reactor of slurry bubble bed |
| CN103285780B (en) * | 2012-02-24 | 2015-07-08 | 北京低碳清洁能源研究所 | Magnetic induction reactor of slurry bubble bed |
| WO2014117723A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| WO2014117725A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| CN106606998A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | Up-flow distributor and up-flow reactor |
| CN106606998B (en) * | 2015-10-23 | 2020-03-24 | 中国石油化工股份有限公司 | Upflow distributor and upflow reactor |
| CN110523350A (en) * | 2018-05-24 | 2019-12-03 | 国家能源投资集团有限责任公司 | The method of paste state bed reactor and F- T synthesis |
| CN111068592A (en) * | 2019-12-30 | 2020-04-28 | 上海睿碳能源科技有限公司 | Slurry bed reactor with multi-stage perforated structure distribution plate |
| CN111068592B (en) * | 2019-12-30 | 2022-04-12 | 上海睿碳能源科技有限公司 | Slurry bed reactor with multi-stage perforated structure distribution plate |
| CN114053961A (en) * | 2020-08-03 | 2022-02-18 | 中国石油化工股份有限公司 | Feeding distributor and reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20121010 |