CN102527298A - Circular ring type continuous feed fixed bed reactor - Google Patents
Circular ring type continuous feed fixed bed reactor Download PDFInfo
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- CN102527298A CN102527298A CN2011104190637A CN201110419063A CN102527298A CN 102527298 A CN102527298 A CN 102527298A CN 2011104190637 A CN2011104190637 A CN 2011104190637A CN 201110419063 A CN201110419063 A CN 201110419063A CN 102527298 A CN102527298 A CN 102527298A
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- fixed bed
- agitated reactor
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- reaction kettle
- circular ring
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- 238000007789 sealing Methods 0.000 claims abstract description 16
- 210000002445 nipple Anatomy 0.000 claims description 27
- 239000007787 solid Substances 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 230000005540 biological transmission Effects 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 abstract description 40
- 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 11
- 238000011069 regeneration method Methods 0.000 description 11
- 239000012530 fluid Substances 0.000 description 8
- 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
- 230000015572 biosynthetic process Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- 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
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000000463 material Substances 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
- 230000005587 bubbling Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000001105 regulatory 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
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- 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
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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 are claimed packed bed reactor again, be filled with solid catalyst or solid reactant, in order to realize a kind of reactor of heterogeneous reaction process.Solid reactant is graininess usually, about particle diameter 2～15mm, is piled into the bed of certain altitude (or thickness), the bed transfixion, and fluid reacts through 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 the realization gas-solid catalysis, and when being used for gas-solid phase or liquid-solid phase uncatalyzed reaction, bed is then loaded solid reactant.
Fixed bed reactors have three kinds of citation forms: (1) is the heat-insulating fixed bed reactors axially.The fluid bed of flowing through from top to bottom vertically, bed is with extraneous no heat exchange.(2) radial adiabatic formula fixed bed reactors.Fluid radially flows through bed, can adopt centrifugal flow or entad flow the together extraneous no heat exchange of bed.(3) calandria type fixed bed reactor is made up of many reaction tube parallel connections.Compare with axial flow reactor, the distance that the radial reactor fluid flows is shorter, and cross section of fluid channel is long-pending bigger, and the pressure of fluid falls less, but the structure of radial reactor is complicated than axial flow reactor.Two kinds of forms of radial reactor and axial flow reactor all belong to adiabatic reactor; Be applicable to that reaction heat effect is little; Or reaction system can bear the occasion of the variations in temperature that is caused by reaction heat effect under the adiabatic condition, and calandria type fixed bed reactor is applicable to the reaction that reaction heat effect is bigger.In addition, the reactor that is formed by above-mentioned citation form tandem compound is arranged still, be called multistage fixed bed reactor.For example: big or when needing segmentation control temperature when reaction heat effect, can a plurality of adiabatic reactors be connected into multistage heat-insulating fixed bed reactors, establish heat exchanger or additional material between the reactor regulating temperature, so that operate under the optimal temperature conditions approaching.
Fixed bed reactors have plurality of advantages: (1) back-mixing is little, and fluid can effectively contact with catalyst, can be than high selectivity when reacting with the series connection side reaction; (2) the catalyst mechanical loss is little; (3) simple in structure.But fixed bed reactors also have its fatal shortcoming, and promptly catalyst can not be changed in the operating process, and catalyst needs the reaction of frequent regeneration generally should not use.Therefore, the heat subject that the continuous type fixed bed reactors become the various countries scholars is made 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,, realize carrying out continuously of charging and reaction through rotation and cellular-type structure regenerated catalyst.
Technical scheme of the present invention is: circular ring type continuous feed fixed bed reactors, comprise air supply pipe 1, and last seal nipple 2, agitated reactor 3, lower seal dish 4, blast pipe 5, rotating disk 6 is formed with rotary tray motor; Agitated reactor 3 radially evenly is divided into the annulus rod structure of a plurality of sector spaces 8 for inner chamber by dividing plate 7, and dock with last seal nipple 2 its upper end, the lower end is sealed by lower seal dish 4; Last seal nipple 2 is separated into the annulus cylindricality seal nipple with agitated reactor 3 corresponding a plurality of sector spaces 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 agitated reactor 3, seal each other and turn between lower seal dish 4 and the agitated reactor 3, it is provided with gas outlet 5 with last seal nipple 2 each corresponding sector space position; Agitated reactor 3 is fixed on the rotating disk 6 through the interior annular distance cover at its center, and the rotary tray motor output shaft connects admittedly through the rotating shaft of common transmission mechanism (like the gear graduation transmission mechanism) with rotating disk 6.Through 3 rotations of driven by motor agitated reactor, realize the 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.
Said going up between seal nipple 2 and the agitated reactor 3 by graphite 10 sealings, between lower seal dish 4 and the agitated reactor 3 through clearance seal and be aided with sealing ring and seal.
The quantity of said agitated reactor 3 inner chamber sector spaces 8 is 4 integral multiple (as 4,8,12 etc.), and the quantity of the quantity of gas outlet and agitated reactor 3 inner chamber sector spaces 8 is consistent on the quantity of last seal nipple 2 inner chamber sector spaces and air inlet and the lower seal dish 4.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 carry out heat exchange through fluid to the heat that produces in the course of reaction at agitated reactor 3 peripheral hardwares displacement thermal sleeve.
The rotary tray motor of this reactor is common commercially available prod, and each air inlet is connected through common pipeline with exhaust outlet, and the material of pipeline, size are looked concrete reaction actual needs and decided.
Operation principle of the present invention is: unstripped gas is fed in first sector space 11 of filling fresh catalyst (reaction zone) by first air inlet, and product is discharged by first exhaust outlet of correspondence and collected; Behind the catalyst reaction inactivation; Drive fan-shaped angle of agitated reactor 3 rotations through motor and rotating disk 6; Make the catalyst behind the inactivation get into second sector space 12 (purge zone I); Feed inert gas by second air inlet, catalyst is replaced, inert gas is discharged emptying by second gas outlet of correspondence; Catalyst after the displacement rotates a fan-shaped angle again by driven by motor agitated reactor 3; Get into the 3rd sector space 13 (renewing zone); Feed regeneration gas by the 3rd air inlet, catalyst is regenerated, the tail gas after the regeneration is by the 3rd gas outlet discharging of correspondence; Catalyst after the regeneration rotates a fan-shaped angle again by driven by motor agitated reactor 3; Get into the 4th sector space 14 (purge zone II); Feed inert gas by the 4th air inlet, catalyst is replaced once more, inert gas is discharged emptying by the 4th gas outlet of correspondence.So circulation; Control the gas flow of each air inlet 1 well; Agitated reactor 3 rotates continuously; Each angle of rotating a sector space (little reative cell), the catalyst granules in the agitated reactor 3 all experience the process of " reaction-purging-regeneration-purging-reaction " in each production cycle, thus the carrying out continuously of realization response.
The present invention has the following advantages:
(1) with the mode of agitated reactor rotation, overcome the deficiency of catalytic reaction discontinuous reaction, realize producing continuously;
(2) utilize agitated reactor to react, can realize large-scale production;
(3) device easy and simple to handle, easy to control, be easy to popularize;
(4) can be used for multiple catalytic reaction, applied range.
Description of drawings
Fig. 1 is a sketch map of the present invention;
Fig. 2 is an agitated reactor sectional schematic diagram of the present invention;
Fig. 3 is the effect sketch map of the single sector space of the present invention;
Fig. 4 is a seal nipple sketch map in the present invention.
Among the figure: the 1-air inlet, the 2-seal nipple, the 3-agitated reactor, 4-lower seal dish, the 5-blast pipe, the 6-rotating disk, the 7-dividing plate, the 8-sector space, the 9-beds, 10-seals graphite, 11-reaction zone, 12-purge zone I, 13-renewing zone, 14-purge zone II.
The specific embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is described further, but said 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, last seal nipple 2, and agitated reactor 3, lower seal dish 4, blast pipe 5, rotating disk 6 is formed with rotary tray motor; Agitated reactor 3 radially evenly is divided into the annulus rod structure of 4 sector spaces 8 for inner chamber by dividing plate 7, and dock with last seal nipple 2 its upper end, the lower end is sealed by lower seal dish 4; Last seal nipple 2 is separated into the annulus cylindricality seal nipple with agitated reactor 3 corresponding 4 sector spaces 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 agitated reactor 3, seal each other and turn between lower seal dish 4 and the agitated reactor 3, it is provided with gas outlet 5 with last seal nipple 2 each corresponding sector space position; Agitated reactor 3 is fixed on the rotating disk 6 through the interior annular distance cover at its center, and the rotary tray motor output shaft connects solid through the rotating shaft of ordinary gear variable transmission mechanism and rotating disk 6.4 air inlets on the last seal nipple 2 are connected with corresponding 4 air supply pipes 1 respectively, and 4 exhaust outlets on the seal disc 4 are connected with corresponding 4 blast pipes 5 respectively.Between last seal nipple 2 and the agitated reactor 3 by graphite 10 sealing, between lower seal dish 4 and the agitated reactor 3 through 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 through common steel tube with exhaust outlet.
Referring to Fig. 4, these fixed bed reactors are used for methane portion oxidation continuous feed reaction.In first sector space 11 of agitated reactor 3, pack the Ce-Fe composite oxides into as the carrier of oxygen in (reaction zone), unstripped gas is a methane.Methane is fed by air inlet 1 and fills in the reaction zone 11 of the fresh carrier of oxygen, and the product synthesis gas is discharged by exhaust outlet 5 and collected.Behind the carrier of oxygen inactivation, by 6 rotations of driven by motor rotating disk, get into adjacent fan section successively, the process of experience " reaction-purging-regeneration-purging-reaction " is carried out partial oxidation reaction of methane continuously.Feed N through air inlet to purge zone
2, the gas in the displacement still; To purge zone bubbling air regeneration gas, carry out Lattice Oxygen regeneration through air inlet.
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.Agitated reactor 3 inner chambers evenly are divided into 12 sector spaces; The quantity of gas outlet is 12 corresponding with agitated reactor 3 on the quantity of last seal nipple 2 inner chamber sector spaces and air inlet and the lower seal dish 4; 12 air inlets on the last seal nipple 2 are connected with corresponding 12 air supply pipes 1 respectively, and 12 exhaust outlets on the 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 through common copper pipe with exhaust outlet.Also be provided with the shell-and-tube heat exchange sleeve outside the agitated reactor 3, the exhaust outlet of renewing zone is connected with the heat exchanger tube air inlet, and the reative cell air inlet pipe is through heat exchange sleeve, by the tail gas preheating reactor feed gas of renewing zone discharge.
Referring to Fig. 4; These fixed bed reactors are used for continuous feed and prepare synthesis gas; Per 4 adjacent sector spaces form the successive reaction unit from " reaction-purging-regeneration-purging-reaction " in the agitated reactor 3, and entire reaction still 3 is made up of three successive reaction unit altogether.Unstripped gas is a methane, and catalyst is the Cu-Zn-Al composite catalyst, and methane feeds the reaction zone of filling the fresh carrier of oxygen by air inlet, and the product synthesis gas is discharged by the gas outlet and collected; Substitution gas is N
2, regeneration gas is a hydrogen, the N after the regeneration
2Discharge by the 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.Agitated reactor 3 inner chambers evenly are divided into 8 sector spaces; The quantity of gas outlet is 8 corresponding with agitated reactor 3 on the quantity of last seal nipple 2 inner chamber sector spaces and air inlet and the lower seal dish 4; 8 air inlets on the last seal nipple 2 are connected with corresponding 8 air supply pipes 1 respectively, and 8 exhaust outlets on the 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 through the common aluminum alloy pipe with exhaust outlet.Also be provided with the shell-and-tube heat exchange sleeve outside the agitated reactor 3, the exhaust outlet of renewing zone is connected with the heat exchanger tube air inlet, and the reative cell air inlet pipe is through heat exchange sleeve, by the tail gas preheating reactor feed gas of renewing zone discharge.
Referring to Fig. 4; These fixed bed reactors are used for continuous feed and prepare synthesis gas; Per 4 adjacent sector spaces form the successive reaction unit from " reaction-purging-regeneration-purging-reaction " in the agitated reactor 3, and entire reaction still 3 is made up of two successive reaction unit altogether.Unstripped gas is a methane, and catalyst is the Cu-Zn-Al composite catalyst, and methane feeds the reaction zone of filling the fresh carrier of oxygen by air inlet, and the product synthesis gas is discharged by the gas outlet and collected; Substitution gas is N
2, regeneration gas is a hydrogen, the N after the regeneration
2Discharge by the gas outlet with hydrogen.
Claims (3)
1. circular ring type continuous feed fixed bed reactors is characterized in that: comprise seal nipple (2), agitated reactor (3), lower seal dish (4), rotating disk (6) and rotary tray motor composition; Agitated reactor (3) radially evenly is divided into the annulus rod structure of a plurality of sector spaces (8) for inner chamber by dividing plate (7), and dock with last seal nipple (2) its upper end, the lower end is sealed by lower seal dish (4); Last seal nipple (2) is separated into the annulus cylindricality seal nipple with the corresponding a plurality of sector spaces of agitated reactor (3) for inner chamber; Its upper end closed and corresponding each sector space position are provided with air inlet, the hatch frame of lower end for dock with agitated reactor (3), seal each other and turn between lower seal dish (4) and the agitated reactor (3), it is provided with the gas outlet with each corresponding sector space position of last seal nipple (2); Agitated reactor (3) is fixed on the rotating disk (6) through the interior annular distance cover at its center; The rotary tray motor output shaft connects solid through the rotating shaft 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: go up between seal nipple (2) and the agitated reactor (3) by graphite (10) sealing, between lower seal dish (4) and the agitated reactor (3) through 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 quantity of agitated reactor (3) inner chamber sector space (8) is 4 integral multiple, and the quantity of the last gas outlet of the quantity of last seal nipple (2) inner chamber sector space and air inlet and lower seal dish (4) and the quantity of agitated reactor (3) inner chamber sector space (8) are consistent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110419063.7A CN102527298B (en) | 2011-12-15 | 2011-12-15 | Circular ring type continuous feed fixed bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110419063.7A CN102527298B (en) | 2011-12-15 | 2011-12-15 | Circular ring type continuous feed fixed bed reactor |
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| CN102527298A true CN102527298A (en) | 2012-07-04 |
| CN102527298B CN102527298B (en) | 2014-09-03 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015120427A3 (en) * | 2014-02-10 | 2015-12-30 | Honeywell International Inc. | Reactor design for liquid phase fluorination |
| 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 |
| CN111111562A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Aromatic ammoxidation combined fluidized bed reaction device and reaction method thereof |
| CN112774581A (en) * | 2021-01-27 | 2021-05-11 | 德艾柯工程技术（上海）有限公司 | Moving bed reactor and using method thereof |
| CN118356875A (en) * | 2024-06-17 | 2024-07-19 | 西安航天源动力工程有限公司 | Packing reactor |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015120427A3 (en) * | 2014-02-10 | 2015-12-30 | Honeywell International Inc. | Reactor design for liquid phase fluorination |
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| CN111111562A (en) * | 2018-10-30 | 2020-05-08 | 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 |
| CN112774581A (en) * | 2021-01-27 | 2021-05-11 | 德艾柯工程技术（上海）有限公司 | Moving bed reactor and using method thereof |
| 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 |
| CN118356875A (en) * | 2024-06-17 | 2024-07-19 | 西安航天源动力工程有限公司 | Packing reactor |
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