CN112774581B - Moving bed reactor and use method thereof - Google Patents
Moving bed reactor and use method thereof Download PDFInfo
- Publication number
- CN112774581B CN112774581B CN202110109096.5A CN202110109096A CN112774581B CN 112774581 B CN112774581 B CN 112774581B CN 202110109096 A CN202110109096 A CN 202110109096A CN 112774581 B CN112774581 B CN 112774581B
- Authority
- CN
- China
- Prior art keywords
- catalyst
- gas phase
- plate
- gap rotary
- moving bed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 91
- 238000007599 discharging Methods 0.000 claims abstract description 30
- 238000011068 loading method Methods 0.000 claims abstract description 17
- 238000011049 filling Methods 0.000 claims abstract description 14
- 238000009826 distribution Methods 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 50
- 239000012071 phase Substances 0.000 description 31
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000000694 effects Effects 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000011343 solid material Substances 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 230000033764 rhythmic process Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
Abstract
The invention relates to a moving bed reactor and a use method thereof, the reactor comprises a reactor shell, a catalyst filling area is arranged in the reactor shell, a catalyst feeding port is arranged at the upper end of the reactor shell, a catalyst discharging port is arranged at the lower end of the reactor shell, the catalyst filling area comprises a gas phase central tube, a plurality of plates surrounding the gas phase central tube, a gap rotary feeding disc arranged at the upper end of the gas phase central tube and a gap rotary discharging disc arranged at the lower end of the gas phase central tube, the plates are axially (circularly) arranged in parallel at equal intervals along the outer tube wall of the gas phase central tube, a plate-type channel is formed between every two adjacent plates, and a gap consistent with the section shape of the plate-type channel is arranged between the gap rotary feeding disc and the gap rotary discharging disc. The reactor can intermittently and continuously load and unload the catalyst, ensure the loading and unloading uniformity of the catalyst, and effectively avoid the problem of uneven axial distribution of air flow.
Description
Technical Field
The invention belongs to the field of chemical equipment, and particularly relates to a moving bed reactor and a using method thereof.
Background
The moving bed reactor is a reactor form for realizing fluid-solid phase contact, solid materials gradually move downwards to the bottom discharge in the reactor under the action of gravity, and the fluid reacts with the solid materials in a contact way. The moving bed reactor has the characteristics of both a fixed bed reactor and a fluidized bed reactor, is particularly suitable for reactions with moderate catalyst deactivation speed and still needs to be recycled. The operation performance of the moving bed reactor and the requirements on the catalyst are both between a fixed bed and a fluidized bed, and compared with the fixed bed, the moving bed reactor has the characteristics of small pressure drop and low investment; compared with an entrained flow bed, the moving bed reactor has the advantages of small back mixing proportion, low pulverization degree of the catalyst, uniform distribution of reaction products, capability of changing the residence time of solids in a larger range, better flexibility and the like. Therefore, the moving bed reactor is widely applied in the fields of chemical processes such as catalytic reforming, gasoline desulfurization, heavy oil lightening, methanol conversion and the like, waste treatment and recovery and the like.
The existing moving bed reactor can be divided into a forward moving bed, a countercurrent moving bed and a cross-flow moving bed according to the relative flow mode of solid materials and gas-phase materials, and researches show that the cross-flow moving bed can obtain a larger ventilation section, and meanwhile, channels of two phases can be separated, so that the reactor has larger application in industrial practice. In the gas-solid cross-flow bed, two abnormal operation phenomena, namely adherence and cavity, can occur, and the two phenomena can influence continuous and stable operation of equipment and even cause device stoppage. The adherence is that the friction force between the catalyst particles on the downstream surface and the wall surface is enough to overcome the gravity because the gas phase flow rate is too large, and the catalyst is not lowered any more; the cavity is formed by separating the catalyst on the upstream surface from the wall surface when the flow rate is too high, and the occurrence of the cavity can lead to uneven axial distribution of air flow in the reactor and even short circuit.
The uniform loading and unloading of the catalyst is also a problem to be solved in the application process of the moving bed reactor, and a valve is generally adopted to control the loading and unloading of the catalyst at present, so that the catalyst in the whole reactor is difficult to uniformly pass through a discharge opening which is far smaller than the diameter of the reactor, uneven loading and unloading of the catalyst can lead to uneven distribution of product gas, and further the operation effect of the whole reactor is affected. In addition, in a moving bed reactor, since the deactivation time of different catalysts varies, the catalyst life is as long as several tens of hundreds of hours and several hours, so that the catalyst replacement frequency varies greatly. The former may employ a batch moving bed reactor, and the latter may employ a continuous moving bed reactor.
Finally, the heat transfer performance of the cross-flow moving bed is always affected, in order to solve the problem, most moving bed reactors adopt a multistage series connection and interstage heat exchange method (CN 102875469A) or a heat exchange method (CN 105218304B) outside the reactor for heat transfer, and the two methods can lead to low space utilization rate of the reactor, large equipment investment and complex operation. It is worth mentioning that the space utilization of the whole reactor is improved, the main cause of the phenomena of wall sticking and cavity sticking is caused, the excessive gas flow rate can be relieved, and the production load requirement can be met at a lower flow rate.
Disclosure of Invention
The invention aims to solve the problems and provide a moving bed reactor and a use method thereof, wherein the catalyst can be intermittently and continuously loaded and unloaded.
The aim of the invention is achieved by the following technical scheme:
the utility model provides a moving bed reactor, this reactor includes the reactor casing, be equipped with the catalyst in the reactor casing and load the district, the upper end of reactor casing is equipped with the catalyst feed inlet, and its lower extreme is equipped with the catalyst discharge opening, the catalyst loads the district including the gas phase center tube, around locating a plurality of plates outside the gas phase center tube, rotate the space rotatory feed tray of locating the gas phase center tube upper end and rotate the space rotatory discharge tray of locating the gas phase center tube lower extreme, the plate is followed the equidistant parallel arrangement of outer tube wall axial of gas phase center tube forms the board passageway between two double-phase adjacent plates, space rotatory feed tray with space rotatory discharge tray be equipped with the breach that the cross-section shape of board passageway is unanimous. The plate-type channels are filled with catalysts, gas enters from the gas-phase central tube and is distributed to the catalyst filling areas of the plate-type channels, and the gap rotary feeding plates and the gap rotary discharging plates are matched with the plate-type channels and used for controlling the loading and unloading speed of the catalysts in the plate-type channels.
Further, the moving bed reactor is a radial reactor, and the reactor shell is cylindrical.
Further, the catalyst feed inlet is provided with a metering buffer tank and a feed inlet conical valve.
Further, the catalyst discharge port is provided with a discharge port cone valve.
Further, the gas phase central tube is a circular tube with gas distribution holes, and the gas phase central tube inlet is connected with the gas phase central tube air inlet.
Further, a gas annular space is formed between the catalyst filling area and the reactor shell, and a gas phase outlet is arranged at the lower end of the gas annular space.
Further, the plate is a rectangular plate, and the width, angle and number of the plate-type channels are adjusted according to the packing layout of the catalyst. The plate-type channel has good sealing performance, ensures that the catalyst moves in the plate-type channel while ensuring the circulation of heating or heat transfer media, and can realize heat exchange in the moving bed reactor in a cross-flow state.
Further, the shape of the gap rotary feeding disc and the gap rotary discharging disc is circular, and the diameter of the gap rotary feeding disc is the same as that of a circle formed by the widths of the central tube and the plate in the gas phase.
Further, the gaps of the gap rotary feeding disc and the gap rotary discharging disc are matched with the plate-type channels, and the rotation of the gap rotary feeding disc and the gap rotary discharging disc realizes continuous or intermittent replacement of the catalyst.
The use method of the moving bed reactor realizes continuous loading and unloading of the catalyst when the notch positions of the gap rotary feeding disc and the gap rotary discharging disc are positioned at the upper end and the lower end of the same plate-type channel and the rotation frequency is consistent; when the gap positions of the gap rotary feeding disc and the gap rotary discharging disc are not at the upper end and the lower end of the same plate-type channel and the rotation frequency is consistent, intermittent loading and unloading of the catalyst are realized, and the interval time is set through the number of staggered plate-type channels.
The specific working principle of the moving bed reactor is that gas phase materials enter from a gas phase central pipe and then are distributed into plate-type channels which are radially distributed to contact with a catalyst for reaction, reaction products enter a gas annular gap and are discharged from an air outlet, and heat exchange medium completes heat exchange through the plate-type channels. By the action of the gravity of the catalyst, when the catalyst needs to be replaced, if the catalyst is deactivated faster, the catalyst needs to be continuously replaced, the catalyst feeding port and the catalyst discharging port are opened, gaps of the gap rotary feeding disc and the gap rotary discharging disc are matched to the same plate-type channel, and then the gap rotary feeding disc and the gap rotary discharging disc rotate in the same direction and at the same speed. If the catalyst activity is longer, only need to change at intervals, match the breach of space rotation feed tray and space rotation discharge tray to different plate-type passageway, after the control accomplishes the change of this passageway catalyst, the syntropy is with the speed removal, and the like is to accomplish the change of whole reactor catalyst.
The invention designs a plate type cross-flow moving bed reactor capable of intermittently and continuously loading and unloading a catalyst. The reactor adopts the gap rotary feeding disc and the gap rotary discharging disc which are well matched with the plate-type channels in the reactor, so that the loading and unloading uniformity of the catalyst can be ensured, and meanwhile, the gap rotary feeding disc and the gap rotary discharging disc can be independently controlled. In addition, the heat exchange in the reactor is realized by the plate structure, the reaction temperature is effectively controlled, and the heat transfer problem is solved; finally, the catalyst in the reactor is filled uniformly and compactly, the space utilization rate of the reactor is improved, the reactor can be operated at a low gas flow rate, and the problem of uneven axial distribution of gas flow and the phenomena of adherence and cavity of the catalyst are effectively avoided.
Compared with the prior art, the invention has the following advantages:
1. due to the adoption of the plate-type catalyst filling channel, the filling of the catalyst is more uniform and compact, the heat exchange in the moving bed reactor is realized, the reaction temperature is accurately controlled, and the space utilization rate of the reactor is improved.
2. The space utilization rate of the reactor is improved, and meanwhile, the catalyst is more uniformly and compactly distributed, so that the reaction load can be achieved at a lower gas flow rate, and abnormal operation phenomena such as wall adhesion, cavity and the like are avoided.
3. Because the gap rotary feeding disc and the gap rotary discharging disc are adopted, the continuous loading and unloading or intermittent loading and unloading of the catalyst can be realized.
4. The plate-type channels are flexible and changeable in arrangement mode and can be adjusted according to process requirements.
5. The gap rotary stripper plate is creatively adopted and perfectly matched with the plate-type reaction channel, so that the catalyst is completely and uniformly unloaded.
6. Because a plurality of channels are used as unit modules for unloading, the catalyst loading and unloading process can be continuously carried out, the rhythm is mild, and the pulverization degree of the catalyst is effectively reduced.
7. The plate pair has smooth surface, mild filling rhythm and difficult bridging formation.
8. Due to the adoption of the cross-flow mode, a larger ventilation cross section is obtained.
Drawings
FIG. 1 is a schematic diagram of a moving bed reactor;
FIG. 2 is a schematic view of the structure of the core tube and plate channels in the gas phase;
FIG. 3 is a schematic diagram of the structure of a void-rotating discharge tray, a void-rotating feed tray, and a gas phase core tube;
in the figure: 1-a catalyst feed inlet; 2-a metering buffer tank; 3-a feed inlet cone valve; 4-gas phase central tube gas inlet; 5-a gas phase core tube; 6-plate type channels; 7-gas annular gap; 8-gas phase outlet; 9-catalyst discharge port; 10-a discharge port cone valve; 11-a gap rotary discharge tray; 12-a void rotation feed tray; 13-reactor housing.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples.
Example 1
Referring to fig. 1, the moving bed reactor comprises a reactor shell 13, a catalyst filling area is arranged in the reactor shell 13, a catalyst feed inlet 1 is arranged at the upper end of the reactor shell 13, a catalyst discharge outlet 9 is arranged at the lower end of the reactor shell, and a metering buffer tank 2 and a feed inlet conical valve 3 are arranged at the catalyst feed inlet 1. The catalyst discharge opening 9 is provided with a discharge opening cone valve 10. The moving bed reactor is a radial reactor and the reactor shell 13 is cylindrical.
As shown in fig. 2 and 3, the plurality of plate pairs and the gas phase central tube form a structure that raw materials radially flow, and the plate-type channels are a catalyst filling area and a raw material reaction area and have the heat exchange function. The catalyst filling area comprises a gas phase central tube 5, a plurality of plates surrounding the gas phase central tube 5, a gap rotary feeding disc 12 rotating on the upper end of the gas phase central tube 5 and a gap rotary discharging disc 11 rotating on the lower end of the gas phase central tube 5, wherein the plates are axially and equidistantly arranged in parallel along the outer tube wall of the gas phase central tube 5, a plate-type channel 6 is formed between every two adjacent plates, and gaps consistent with the cross section shape of the plate-type channel 6 are formed in the gap rotary feeding disc 12 and the gap rotary discharging disc 11. The gas phase central tube 5 is a breathable circular tube, and the inlet of the gas phase central tube 5 is connected with the gas inlet 4 of the gas phase central tube. A gas annular space 7 is formed between the catalyst filling area and the reactor shell 13, and a gas phase outlet 8 is arranged at the lower end of the gas annular space 7. The plates are rectangular plates, and the width, angle and number of the plate channels 6 are adjusted according to the packing layout of the catalyst. The gap rotary feeding disc 12 and the gap rotary discharging disc 11 are circular in shape, and the diameter is the same as the circular diameter formed by the gas phase central tube 5 and the width of the plate. The gaps of the gap rotary feeding disc 12 and the gap rotary discharging disc 11 are matched with the plate-type channel 6, and the rotation of the gap rotary feeding disc 12 and the gap rotary discharging disc 11 realizes continuous or intermittent replacement of the catalyst. When the gap positions of the gap rotary feeding disc 12 and the gap rotary discharging disc 11 are positioned at the upper end and the lower end of the same plate-type channel 6 and the rotation frequency is consistent, continuous loading and unloading of the catalyst are realized; when the gap positions of the gap rotary feeding disc 12 and the gap rotary discharging disc 11 are not at the upper end and the lower end of the same plate-type channel 6 and the rotation frequency is consistent, intermittent loading and unloading of the catalyst are realized, and the interval time is set by the number of staggered plate-type channels 6.
Example 2
The invention is further described by taking xylene isomerization reaction as an example, wherein the mixed gas of raw material liquid, high-temperature solvent and carrier gas enters a gas phase central tube 5 from a gas phase central tube gas inlet 4, then is distributed to each plate-type channel 6 to contact with a catalyst for reaction, the product enters a gas annular space 7, and then is discharged from a gas phase outlet 8 to enter downstream separation and refining to obtain the xylene isomerization product. If the activity of the catalyst can not meet the reaction requirement, firstly placing the regenerated or fresh catalyst into a metering buffer tank 2, opening a feed inlet conical valve 3 and a discharge outlet conical valve 10, and enabling the activity life time of the catalyst to be longer; if the catalyst is deactivated in two hours for catalytic reforming reaction, the catalyst is always in a flowing state in the reaction process, and the gaps of the gap rotary feeding disc 12 and the gap rotary discharging disc 11 are matched to the same plate-type channel 6, and then the catalyst rotates in the same direction and at the same speed.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present invention.
Claims (9)
1. The moving bed reactor comprises a reactor shell (13), wherein a catalyst filling area is arranged in the reactor shell (13), a catalyst feeding hole (1) is arranged at the upper end of the reactor shell (13), a catalyst discharging hole (9) is arranged at the lower end of the reactor shell,
it is characterized in that the reactor is a cross-flow moving bed reactor, the catalyst filling area comprises a gas phase central tube (5), a plurality of plates which are arranged outside the gas phase central tube (5) in a surrounding way, a gap rotary feeding disc (12) which is arranged at the upper end of the gas phase central tube (5) and a gap rotary discharging disc (11) which is arranged at the lower end of the gas phase central tube (5),
the plates are arranged in parallel at equal intervals along the outer pipe wall of the gas phase central pipe (5), a plate-type channel (6) is formed between every two adjacent plates, a gap rotary feeding plate (12) and a gap rotary discharging plate (11) are provided with gaps which are consistent with the section shape of the plate-type channel (6), the plate-type channel (6) is filled with a catalyst,
the gaps of the gap rotary feeding disc (12) and the gap rotary discharging disc (11) are matched with the plate-type channels (6), the rotation of the gap rotary feeding disc (12) and the gap rotary discharging disc (11) realizes continuous or intermittent replacement of the catalyst,
the gas phase material enters from the gas phase central pipe (5) and then is distributed into the catalyst filling area of the plate-type channel (6) to contact and react with the catalyst.
2. A moving bed reactor according to claim 1, characterized in that the moving bed reactor is a loop reactor, and the reactor shell (13) is cylindrical.
3. Moving bed reactor according to claim 1, characterized in that the catalyst feed (1) is provided with a metering buffer tank (2) and a feed cone valve (3).
4. Moving bed reactor according to claim 1, characterized in that the catalyst discharge opening (9) is provided with a discharge opening cone valve (10).
5. Moving bed reactor according to claim 1, characterized in that the gas phase center tube (5) is a circular tube with gas distribution holes, and the inlet of the gas phase center tube (5) is connected with the gas phase center tube gas inlet (4).
6. Moving bed reactor according to claim 5, characterized in that a gas annulus (7) is formed between the catalyst loading zone and the reactor shell (13), the lower end of the gas annulus (7) being provided with a gas phase outlet (8).
7. A moving bed reactor according to claim 1, characterized in that the plates are rectangular plates, the width, angle and number of the plate channels (6) being adjusted according to the packing layout of the catalyst.
8. Moving bed reactor according to claim 1, characterized in that the gap rotary feed tray (12) and the gap rotary discharge tray (11) are circular in shape with the same diameter as the circular diameter formed by the gas phase center tube (5) and the width of the plate.
9. A method of using a moving bed reactor as claimed in any one of claims 1 to 8,
when the gap positions of the gap rotary feeding disc (12) and the gap rotary discharging disc (11) are positioned at the upper end and the lower end of the same plate-type channel (6) and the rotation frequencies are consistent, continuous loading and unloading of the catalyst are realized;
when the gap positions of the gap rotary feeding disc (12) and the gap rotary discharging disc (11) are not at the upper end and the lower end of the same plate-type channel (6) and the rotation frequency is consistent, intermittent loading and unloading of the catalyst are realized, and the interval time is set through the number of staggered plate-type channels (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110109096.5A CN112774581B (en) | 2021-01-27 | 2021-01-27 | Moving bed reactor and use method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110109096.5A CN112774581B (en) | 2021-01-27 | 2021-01-27 | Moving bed reactor and use method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112774581A CN112774581A (en) | 2021-05-11 |
| CN112774581B true CN112774581B (en) | 2023-11-21 |
Family
ID=75758168
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110109096.5A Active CN112774581B (en) | 2021-01-27 | 2021-01-27 | Moving bed reactor and use method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112774581B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114558521B (en) * | 2022-03-10 | 2023-01-10 | 无锡碳谷科技有限公司 | Layered material distribution moving bed reaction device and use method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201586520U (en) * | 2009-04-14 | 2010-09-22 | 中国科学院山西煤炭化学研究所 | Moving bed reactor |
| CN102527298A (en) * | 2011-12-15 | 2012-07-04 | 昆明理工大学 | Circular ring type continuous feed fixed bed reactor |
| CN202410624U (en) * | 2011-12-15 | 2012-09-05 | 昆明理工大学 | Ring-shaped continuous feeding fixed bed reactor |
| CN202683181U (en) * | 2012-06-21 | 2013-01-23 | 中国石油化工集团公司 | Continuous reforming reactor with charging hopper |
| CN103301785A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Gas phase catalytic reaction method as well as moving-bed reactor and applications thereof |
| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
| CN105617946A (en) * | 2014-10-27 | 2016-06-01 | 中国石油化工股份有限公司 | Moving bed radial flow reactor and application thereof |
-
2021
- 2021-01-27 CN CN202110109096.5A patent/CN112774581B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201586520U (en) * | 2009-04-14 | 2010-09-22 | 中国科学院山西煤炭化学研究所 | Moving bed reactor |
| CN102527298A (en) * | 2011-12-15 | 2012-07-04 | 昆明理工大学 | Circular ring type continuous feed fixed bed reactor |
| CN202410624U (en) * | 2011-12-15 | 2012-09-05 | 昆明理工大学 | Ring-shaped continuous feeding fixed bed reactor |
| CN103301785A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Gas phase catalytic reaction method as well as moving-bed reactor and applications thereof |
| CN202683181U (en) * | 2012-06-21 | 2013-01-23 | 中国石油化工集团公司 | Continuous reforming reactor with charging hopper |
| CN105617946A (en) * | 2014-10-27 | 2016-06-01 | 中国石油化工股份有限公司 | Moving bed radial flow reactor and application thereof |
| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112774581A (en) | 2021-05-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8071059B2 (en) | Chemical reactor | |
| CN101653710B (en) | Multistage multi-channel radial adiabatic reactor | |
| CN101274245B (en) | Annular space air-lift gas-solid loop flow reactor | |
| JPH045488B2 (en) | ||
| CN112774581B (en) | Moving bed reactor and use method thereof | |
| CN101001691A (en) | Fixed-bed catalytic reactor | |
| CN203990548U (en) | radial parallel catalytic reactor | |
| CN101116804A (en) | Integrated reacting and separating device | |
| CN105032305A (en) | Novel radial plate type reactor | |
| CN101422716A (en) | Method and apparatus for improving radial flow moving bed regeneration/reaction system performance | |
| CN204193907U (en) | A kind of monolith honeycomb reactor for gas-liquid-solid reaction system | |
| CN203507983U (en) | Novel radial fixed bed reactor of multi-layer bed | |
| US2704741A (en) | Method and apparatus for conversion of organic reactants to other organic products | |
| EP0269171B1 (en) | Reactor for exothermic and endothermic catalytic reactions | |
| KR101672601B1 (en) | Dehydogenation reactor | |
| CN115591480A (en) | Radial moving bed reactor and process for producing caprolactam | |
| CN204933424U (en) | A kind of novel radial plate-type reactor | |
| CN212348666U (en) | Radial flow fixed bed catalytic reactor for generating oxalate through CO carbonylation coupling | |
| CN214810704U (en) | Gas-liquid-solid three-phase or liquid-solid two-phase radial flow reactor | |
| CN107551961B (en) | High-temperature high-pressure slurry bed reaction device | |
| CN209663242U (en) | Reaction unit | |
| CN202983653U (en) | Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene | |
| CN211026224U (en) | Radial moving bed reaction system | |
| CN107224939B (en) | Axial reactor | |
| CN111589378A (en) | Radial flow fixed bed catalytic reactor for generating oxalate through CO carbonylation coupling |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |