CN102527298B - Circular ring type continuous feed fixed bed reactor - Google Patents
Circular ring type continuous feed fixed bed reactor Download PDFInfo
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- CN102527298B CN102527298B CN201110419063.7A CN201110419063A CN102527298B CN 102527298 B CN102527298 B CN 102527298B CN 201110419063 A CN201110419063 A CN 201110419063A CN 102527298 B CN102527298 B CN 102527298B
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- reactor
- fixed bed
- seal
- reaction kettle
- circular ring
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- 238000007789 sealing Methods 0.000 claims abstract description 13
- 210000002445 nipple Anatomy 0.000 claims description 27
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 38
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000003197 catalytic effect Effects 0.000 abstract description 2
- 230000007812 deficiency Effects 0.000 abstract description 2
- 238000011031 large-scale manufacturing process Methods 0.000 abstract description 2
- 210000001503 joint Anatomy 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 34
- 239000003054 catalyst Substances 0.000 description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- 230000008929 regeneration Effects 0.000 description 10
- 238000011069 regeneration method Methods 0.000 description 10
- 239000012530 fluid Substances 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000010926 purge Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000006073 displacement reaction Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 230000002779 inactivation Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 229910017773 Cu-Zn-Al Inorganic materials 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005755 formation reaction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- 241000784732 Lycaena phlaeas Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention provides a circular ring type continuous feed fixed bed reactor, which belongs to the technical field of catalytic fixed bed reactors, and comprises an upper sealing connector, a reaction kettle, a lower sealing disc, a rotary disc and a rotary disc motor. The cavity of the reaction kettle is divided into a plurality of fan-shaped spaces by a separator. The upper end of the reaction kettle is in butt joint with the upper sealing connector while the lower end is sealed by the lower sealing disc. The upper sealing connector is a circular cylindrical sealing connector corresponding to the reaction kettle. The upper end of the upper sealing connector is sealed and provided with an air inlet corresponding to each fan-shaped space position while the lower end is an opening structure in butt joint with the reaction kettle. The lower sealing disc and the reaction kettle are sealed with each other and rotatable. The lower sealing disc is provided with an air outlet at each fan-shaped space position corresponding to the upper sealing connector. The reaction kettle is sleeved and fixed on the rotary disc through an inner circular hole. The air inlets and air outlets are connected with corresponding air supply pipes and air discharge pipes respectively. While maintaining the advantages of stable production and large processing capacity of the fixed bed reactor, the circular ring type continuous feed fixed bed reactor overcomes the deficiency that current fixed bed reactor cannot produce continuously, so as to realize efficient, energy-saving, continuous, stable and large-scale production.
Description
Technical field
The present invention relates to a kind of circular ring type continuous feed fixed bed reactors, belong to catalytic fixed bed reactor technology field.
Technical background
Fixed bed reactors claim again packed bed reactor, be filled with solid catalyst or solid reactant, in order to realize a kind of reactor of heterogeneous reaction process.Solid reactant is graininess conventionally, about particle diameter 2～15mm, is piled into the bed of certain altitude (or thickness), bed transfixion, and fluid reacts by bed.The difference of fixed bed reactors and fluidized-bed reactor and moving-burden bed reactor is that solid particle remains static.Fixed bed reactors are mainly used in realizing gas-solid catalysis, and during for gas-solid phase or liquid-solid phase uncatalyzed reaction, bed is loaded solid reactant.
Fixed bed reactors have three kinds of citation forms: (1) is heat-insulating fixed bed reactors axially.The fluid bed of flowing through from top to bottom vertically, bed with extraneous without heat exchange.(2) radial adiabatic formula fixed bed reactors.Fluid radially flows through bed, can adopt centrifugal flow or centripetal flow, and bed is same extraneous without heat exchange.(3) calandria type fixed bed reactor, consists of many reaction tube parallel connections.Compare with axial flow reactor, the mobile distance of radial reactor fluid is shorter, and cross section of fluid channel is long-pending larger, and the Pressure Drop of fluid is less, but the structure of radial reactor is complicated compared with axial flow reactor.Two kinds of forms of radial reactor and axial flow reactor all belong to adiabatic reactor, be applicable to reaction heat effect little, or reaction system can bear the occasion of the variations in temperature being caused by reaction heat effect under adiabatic condition, and calandria type fixed bed reactor is applicable to the reaction that reaction heat effect is larger.In addition, still there is the reactor being formed by above-mentioned citation form tandem compound, be called multistage fixed bed reactor.For example: when reaction heat effect is large or need segmentation to control temperature, a plurality of adiabatic reactors can be connected into multistage heat-insulating fixed bed reactors, between reactor, establish heat exchanger or supplementary material to regulate temperature, to operating close under optimal temperature conditions.
Fixed bed reactors have plurality of advantages: (1) back-mixing is little, and fluid can effectively contact with catalyst, can be compared with high selectivity when reacting with series connection side reaction; (2) catalyst mechanical loss is little; (3) simple in structure.But fixed bed reactors also have its fatal shortcoming, and in operating process, catalyst can not be changed, catalyst needs the reaction of frequent regeneration generally should not use.Therefore, the heat subject that continuous type fixed bed reactors become various countries scholars is manufactured in research.
Summary of the invention
The object of the present invention is to provide a kind of circular ring type continuous feed fixed bed reactors, by rotation and partition structure regenerated catalyst, realize carrying out continuously of charging and reaction.
Technical scheme of the present invention is: circular ring type continuous feed fixed bed reactors, comprise air supply pipe 1, and upper seal nipple 2, reactor 3, lower seal dish 4, blast pipe 5, rotating disk 6 and rotary tray motor form; Reactor 3 is radially evenly divided into the annulus rod structure of a plurality of sector spaces 8 for inner chamber by dividing plate 7, dock with upper seal nipple 2 its upper end, lower end is sealed by lower seal dish 4; The annulus cylindricality seal nipple of a plurality of sector spaces that upper seal nipple 2 is corresponding with reactor 3 for inner chamber is separated into, its upper end closed and corresponding each sector space position are provided with air inlet 1, the hatch frame of lower end for dock with reactor 3, between lower seal dish 4 and reactor 3, mutually seal and rotatably, it is provided with gas outlet 5 with each sector space position corresponding to upper seal nipple 2; Reactor 3 is fixed on rotating disk 6 by the interior annular distance cover at its center, and rotary tray motor output shaft is the rotating shaft fixed with rotating disk 6 by common transmission mechanism (as speed-changing gear driving device).By 3 rotations of driven by motor reactor, realize regeneration and the displacement of sector space inner catalyst.Each air inlet is connected with corresponding air supply pipe 1 respectively, and each exhaust outlet is connected with corresponding blast pipe 5 respectively.
Between described upper seal nipple 2 and reactor 3, by graphite 10, sealed, between lower seal dish 4 and reactor 3 by clearance seal and be aided with sealing ring and seal.
The integral multiple that the quantity of described reactor 3 inner chamber sector spaces 8 is 4 (as 4,8,12 etc.), on the quantity of upper seal nipple 2 inner chamber sector spaces and air inlet and lower seal dish 4, the quantity of gas outlet is consistent with the quantity of reactor 3 inner chamber sector spaces 8.Can specifically adjust the quantity of sector space 8 according to different reaction actual needs, realize continuous, steady production.
According to actual needs, also can, at reactor 3 peripheral hardware displacement thermal sleeves, by fluid, to the heat producing in course of reaction, carry out heat exchange.
The rotary tray motor of this reactor is common commercially available prod, and each air inlet is connected by common pipeline with exhaust outlet, and the material of pipeline, size are depending on concrete reaction actual needs.
Operation principle of the present invention is: unstripped gas, by first air inlet, passes in first sector space 11 of filling fresh catalyst (reaction zone), and product is discharged and collected by first exhaust outlet of correspondence; After catalyst reaction inactivation, by motor and rotating disk 6, drive a fan-shaped angle of reactor 3 rotations, make the catalyst after inactivation enter second sector space 12(purge zone I), by second air inlet, pass into inert gas, catalyst is replaced, and inert gas is discharged emptying by second gas outlet of correspondence; Catalyst after displacement rotates a fan-shaped angle again by driven by motor reactor 3, enter the 3rd sector space 13(renewing zone), by the 3rd air inlet, pass into regeneration gas, catalyst is regenerated, the tail gas after regeneration is discharged by the 3rd gas outlet of correspondence; Catalyst after regeneration rotates a fan-shaped angle again by driven by motor reactor 3, enter the 4th sector space 14(purge zone II), by the 4th air inlet, pass into inert gas, catalyst is replaced again, inert gas is discharged emptying by the 4th gas outlet of correspondence.So circulation, control the gas flow of each air inlet 1 well, reactor 3 rotates continuously, each angle of rotating a sector space (little reative cell), catalyst granules in reactor 3 experiences the process of " reaction-purge-regeneration-purging-reaction " within each production cycle, thus the carrying out continuously of realization response.
The present invention has the following advantages:
(1) in the mode of reactor rotation, overcome the deficiency of catalytic reaction discontinuous reaction, realize continuously and producing;
(2) utilize reactor to react, can realize large-scale production;
(3) install easy and simple to handle, easy to control, be easy to popularize;
(4) can be used for multiple catalytic reaction, applied range.
Accompanying drawing explanation
Fig. 1 is schematic diagram of the present invention;
Fig. 2 is reactor sectional schematic diagram of the present invention;
Fig. 3 is the effect schematic diagram of the single sector space of the present invention;
Fig. 4 is seal nipple schematic diagram in the present invention.
In figure: 1-air inlet, 2-seal nipple, 3-reactor, 4-lower seal dish, 5-blast pipe, 6-rotating disk, 7-dividing plate, 8-sector space, 9-beds, 10-sealed graphite, 11-reaction zone, 12-purge zone I, 13-renewing zone, 14-purge zone II.
The specific embodiment
Below in conjunction with drawings and Examples, the invention will be further described, but described content is not construed as limiting the invention.
Embodiment 1: referring to Fig. 1-3, this circular ring type continuous feed fixed bed reactors, comprise air supply pipe 1, upper seal nipple 2, and reactor 3, lower seal dish 4, blast pipe 5, rotating disk 6 and rotary tray motor form; Reactor 3 is radially evenly divided into the annulus rod structure of 4 sector spaces 8 for inner chamber by dividing plate 7, dock with upper seal nipple 2 its upper end, lower end is sealed by lower seal dish 4; Upper seal nipple 2 is separated into the annulus cylindricality seal nipple of 4 sector spaces corresponding with reactor 3 for inner chamber, its upper end closed and corresponding each sector space position are provided with air inlet 1, the hatch frame of lower end for dock with reactor 3, between lower seal dish 4 and reactor 3, mutually seal and rotatably, it is provided with gas outlet 5 with each sector space position corresponding to upper seal nipple 2; Reactor 3 is fixed on rotating disk 6 by the interior annular distance cover at its center, and rotary tray motor output shaft is by the rotating shaft fixed of ordinary gear variable transmission mechanism and rotating disk 6.4 air inlets on upper seal nipple 2 are connected with corresponding 4 air supply pipes 1 respectively, and 4 exhaust outlets on seal disc 4 are connected with corresponding 4 blast pipes 5 respectively.Between upper seal nipple 2 and reactor 3, by graphite 10, sealed, between lower seal dish 4 and reactor 3 by clearance seal and be aided with sealing ring and seal.Rotary tray motor adopts ordinary city sale of electricity machine, and each air inlet is connected by common steel tube with exhaust outlet.
Referring to Fig. 4, these fixed bed reactors are for methane portion oxidation continuous feed reaction.In first sector space 11 of reactor 3, in (reaction zone), pack Ce-Fe composite oxides into as the carrier of oxygen, unstripped gas is methane.Methane is passed into by air inlet 1 in the reaction zone 11 of filling the fresh carrier of oxygen, and product synthesis gas is discharged and collected by exhaust outlet 5.After carrier of oxygen inactivation, by 6 rotations of driven by motor rotating disk, enter successively adjacent fan section, the process of experience " reaction-purging-regeneration-purging-reaction ", carries out partial oxidation reaction of methane continuously.By air inlet, to purge zone, pass into N
2, the gas in displacement still; By air inlet, to purge zone, pass into air regenesis gas, carry out Lattice Oxygen regeneration.
Embodiment 2: referring to Fig. 1-3, the agent structure of this circular ring type continuous feed fixed bed reactors is identical with embodiment 1.Reactor 3 inner chambers are evenly divided into 12 sector spaces; On the quantity of upper seal nipple 2 inner chamber sector spaces and air inlet and lower seal dish 4, the quantity of gas outlet is 12 corresponding with reactor 3; 12 air inlets on upper seal nipple 2 are connected with corresponding 12 air supply pipes 1 respectively, and 12 exhaust outlets on seal disc 4 are connected with corresponding 12 blast pipes 5 respectively.Rotary tray motor adopts ordinary city sale of electricity machine, and each air inlet is connected by common copper pipe with exhaust outlet.Reactor 3 is outer is also provided with pipe shell type heat exchange sleeve pipe, and the exhaust outlet of renewing zone is connected with heat exchanger tube air inlet, and reative cell air inlet pipe is through heat exchange sleeve, the tail gas preheating reactor feed gas of being discharged by renewing zone.
Referring to Fig. 4, these fixed bed reactors are prepared synthesis gas for continuous feed, in reactor 3, every 4 adjacent sector spaces form one from the successive reaction unit of " reaction-purging-regeneration-purging-reaction ", and whole reactor 3 is altogether by three successive reaction cell formations.Unstripped gas is methane, and catalyst is Cu-Zn-Al composite catalyst, and methane is passed into the reaction zone of filling the fresh carrier of oxygen by air inlet, and product synthesis gas is discharged and collected by gas outlet; Substitution gas is N
2, regeneration gas is hydrogen, the N after regeneration
2discharged by gas outlet with hydrogen.
Embodiment 3: referring to Fig. 1-3, the agent structure of this circular ring type continuous feed fixed bed reactors is identical with embodiment 1.Reactor 3 inner chambers are evenly divided into 8 sector spaces; On the quantity of upper seal nipple 2 inner chamber sector spaces and air inlet and lower seal dish 4, the quantity of gas outlet is 8 corresponding with reactor 3; 8 air inlets on upper seal nipple 2 are connected with corresponding 8 air supply pipes 1 respectively, and 8 exhaust outlets on seal disc 4 are connected with corresponding 8 blast pipes 5 respectively.Rotary tray motor adopts ordinary city sale of electricity machine, and each air inlet is connected by common aluminum alloy pipe with exhaust outlet.Reactor 3 is outer is also provided with pipe shell type heat exchange sleeve pipe, and the exhaust outlet of renewing zone is connected with heat exchanger tube air inlet, and reative cell air inlet pipe is through heat exchange sleeve, the tail gas preheating reactor feed gas of being discharged by renewing zone.
Referring to Fig. 4, these fixed bed reactors are prepared synthesis gas for continuous feed, in reactor 3, every 4 adjacent sector spaces form one from the successive reaction unit of " reaction-purging-regeneration-purging-reaction ", and whole reactor 3 is altogether by two successive reaction cell formations.Unstripped gas is methane, and catalyst is Cu-Zn-Al composite catalyst, and methane is passed into the reaction zone of filling the fresh carrier of oxygen by air inlet, and product synthesis gas is discharged and collected by gas outlet; Substitution gas is N
2, regeneration gas is hydrogen, the N after regeneration
2discharged by gas outlet with hydrogen.
Claims (3)
1. circular ring type continuous feed fixed bed reactors, is characterized in that: comprise seal nipple (2), reactor (3), lower seal dish (4), rotating disk (6) and rotary tray motor composition; Reactor (3) is radially evenly divided into the annulus rod structure of a plurality of sector spaces (8) for inner chamber by dividing plate (7), dock with upper seal nipple (2) its upper end, lower end is sealed by lower seal dish (4); The annulus cylindricality seal nipple of upper seal nipple (2) a plurality of sector spaces corresponding with reactor (3) for inner chamber is separated into, its upper end closed and corresponding each sector space position are provided with air inlet, the hatch frame of lower end for dock with reactor (3), between lower seal dish (4) and reactor (3), mutually seal and rotatably, it is provided with gas outlet with each sector space position corresponding to upper seal nipple (2); Reactor (3) is fixed on rotating disk (6) by the interior annular distance cover at its center, rotary tray motor output shaft is by the rotating shaft fixed of transmission mechanism and rotating disk (6), each air inlet is connected with corresponding air supply pipe (1) respectively, and each exhaust outlet is connected with corresponding blast pipe (5) respectively.
2. circular ring type continuous feed fixed bed reactors according to claim 1, it is characterized in that: between upper seal nipple (2) and reactor (3), by graphite (10), sealed, between lower seal dish (4) and reactor (3) by clearance seal and be aided with sealing ring and seal.
3. circular ring type continuous feed fixed bed reactors according to claim 1, it is characterized in that: the integral multiple that the quantity of reactor (3) inner chamber sector space (8) is 4, the quantity of the upper gas outlet of the quantity of upper seal nipple (2) inner chamber sector space and air inlet and lower seal dish (4) is consistent with the quantity of reactor (3) inner chamber sector space (8).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110419063.7A CN102527298B (en) | 2011-12-15 | 2011-12-15 | Circular ring type continuous feed fixed bed reactor |
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| CN201110419063.7A CN102527298B (en) | 2011-12-15 | 2011-12-15 | Circular ring type continuous feed fixed bed reactor |
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| CN102527298A CN102527298A (en) | 2012-07-04 |
| CN102527298B true CN102527298B (en) | 2014-09-03 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20150225315A1 (en) * | 2014-02-10 | 2015-08-13 | Honeywell International Inc. | Reactor design for liquid phase fluorination |
| CN111111562B (en) * | 2018-10-30 | 2022-08-12 | 中国石油化工股份有限公司 | Aromatic ammoxidation combined fluidized bed reaction device and reaction method thereof |
| CN109833833A (en) * | 2019-04-08 | 2019-06-04 | 江苏扬农化工集团有限公司 | A kind of the propylene oxide synthesizer and method of continuous reproducible catalyst |
| CN112774581B (en) * | 2021-01-27 | 2023-11-21 | 德艾柯工程技术（上海）有限公司 | Moving bed reactor and use method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0483975A1 (en) * | 1990-10-03 | 1992-05-06 | Nagaoka International Corporation | Device and method for holding catalyst in a radial flow reactor |
| CN1350878A (en) * | 2000-10-26 | 2002-05-29 | 中国石油化工股份有限公司 | Process for removing acidic gas by adsorption |
| CN1393278A (en) * | 2001-07-02 | 2003-01-29 | 中国石油化工股份有限公司 | Adsorptive process for removing acidic stink gas |
| CN201534043U (en) * | 2009-11-12 | 2010-07-28 | 福建嘉园环保有限责任公司 | Integrated rotary adsorption and desorption organic waste gas treatment device |
| CN202410624U (en) * | 2011-12-15 | 2012-09-05 | 昆明理工大学 | Ring-shaped continuous feeding fixed bed reactor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1300190A1 (en) * | 2001-10-04 | 2003-04-09 | Methanol Casale S.A. | Heterogeneous catalytic reactor with modular catalytic cartridge |
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2011
- 2011-12-15 CN CN201110419063.7A patent/CN102527298B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0483975A1 (en) * | 1990-10-03 | 1992-05-06 | Nagaoka International Corporation | Device and method for holding catalyst in a radial flow reactor |
| CN1350878A (en) * | 2000-10-26 | 2002-05-29 | 中国石油化工股份有限公司 | Process for removing acidic gas by adsorption |
| CN1393278A (en) * | 2001-07-02 | 2003-01-29 | 中国石油化工股份有限公司 | Adsorptive process for removing acidic stink gas |
| CN201534043U (en) * | 2009-11-12 | 2010-07-28 | 福建嘉园环保有限责任公司 | Integrated rotary adsorption and desorption organic waste gas treatment device |
| CN202410624U (en) * | 2011-12-15 | 2012-09-05 | 昆明理工大学 | Ring-shaped continuous feeding fixed bed reactor |
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