CN107519822A - A kind of multi-bed layer shaft radial reactor - Google Patents
A kind of multi-bed layer shaft radial reactor Download PDFInfo
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- CN107519822A CN107519822A CN201610454666.3A CN201610454666A CN107519822A CN 107519822 A CN107519822 A CN 107519822A CN 201610454666 A CN201610454666 A CN 201610454666A CN 107519822 A CN107519822 A CN 107519822A
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- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- 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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/027—Beds
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- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a kind of multi-bed layer shaft radial reactor, the reactor includes radial direction cylindrical shape seal and pressure bearing housing (2), air inlet pipe (16), Axial and radial catalytic reaction zone (8) and escape pipe (14)；The Axial and radial catalytic reaction zone (8) for can containing catalyst bed cylindrical shape receiving space, the shell of the receiving space is formed by side wall (11), top end socket (5) and back cover (18), wherein described side wall (11) and the selectively back cover (18) are fluid-impermeable but the impermeable open-celled structure of solid catalyst, and the top end socket (5) is the impermeable structure of fluid.The reactor pressure decrease is low, space availability ratio is high, without gas bias current and short circuit phenomenon.
Description
Technical field
The present invention relates to a kind of multi-bed layer shaft radial reactor.
Background technology
Fixed bed reactors mainly have two types, and one kind is axially-located bed reactor, and another kind is radial fixed-bed
Reactor.Axially-located bed reactor design, process are relatively easy, simple to operate, but reactor apparatus size Pang be present
Greatly, bed pressure drop is big, local run aways easily occurs, moves the problems such as heat is slow, conversion ratio is low, enlarge-effect is obvious.Radial bed is anti-
Answer utensil have ratio of height to diameter is larger, bed pressure drop is small, reactant the beds residence time is short, operating cost is low, production energy
Power is high, and catalyst particle can be used, and is easy to the advantages such as maximization, but reactant difficult to realize being uniformly distributed diametrically.
The quality of radial bed reactor design has a great influence to course of reaction.Axially uniform problem is real to fluid in bed
The key problem in technology of existing such reactor optimization design.Whether uniform reactant distribution is, is directly related to conversion ratio, the production of reactant
The selectivity of thing and the operational stability of reactor.Zhang Chengfang et al. (researchs (II) of radial reactor uniform fluid distribution design
[J] Chemical Engineerings, 1980,2 (2):82-89.), Wang Jinfu et al. (reforms the fluid force scholarship and moral conduct of radial reactor gas distribution system
For and its optimization design [J] petroleum refinings and chemical industry, 1997,28 (4):47-52.) propose radial reactor uniform fluid distribution
Method.In general, uniform fluid distribution is mainly the side controlled by choosing appropriate runner, mass flow pathway form and percent opening
Method realizes the uniform of convection body.
Therefore, in order to further improve the fluid uniformity of radial reactor, meet what radial reactor constantly maximized
Growth requirement is still technical problem urgently to be resolved hurrily at present, while is also the developing direction of following radial fixed-bed reactor.
The content of the invention
It is an object of the invention to provide a kind of multi-bed layer shaft radial reactor, the reactor pressure decrease is low, space availability ratio is high,
Without gas bias current and short circuit phenomenon.
To achieve these goals, the present invention provides a kind of multi-bed layer shaft radial reactor, and the reactor includes radially circle
Shaped seals pressure-bearing shell, extend into from the case top air inlet pipe of enclosure interior, be arranged in the housing it is described enter
The Axial and radial catalytic reaction zone coaxial with housing and escape pipe below tracheae；The Axial and radial catalytic reaction zone is to hold
Receive the cylindrical shape receiving spaces of beds, the shell of the receiving space is formed by side wall, top end socket and back cover, wherein institute
State side wall and selectively the back cover is fluid-impermeable but the impermeable open-celled structure of solid catalyst, the top
End socket is the impermeable structure of fluid；One end of the escape pipe is sealedly attached to the top envelope of Axial and radial catalytic reaction zone
Head and reaches the outer of the housing with the internal fluid communication of the Axial and radial catalytic reaction zone, the other end sealing of escape pipe
Portion；Formed with annular space, the air inlet pipe and institute between the side wall of the Axial and radial catalytic reaction zone and the madial wall of the housing
State annular fluid connection.
Preferably, the Axial and radial catalytic reaction zone has central tube, and the central tube is tightly connected with the escape pipe
And be in fluid communication, the end being connected with the top end socket of the central tube is the impermeable structure of fluid, the stream of central tube
Part below the end of the impermeable structure of body is fluid-impermeable but the impermeable open-celled structure of solid catalyst.
Preferably, in the receiving space of the Axial and radial catalytic reaction zone also include with housing it is coaxial and with the appearance
At least one cylindrical gas that the side wall of the shell in space and the shape of back cover match of receiving redistributes plate, described
The end sealing of gas redistribution plate is fixed on the top end socket；The shell of the receiving space and outermost institute
State between gas redistribution plate, the gas redistribution plate of between adjacent two gas redistribution plate and most inner side
Formed with catalyst bed sheaf space between the central tube；The end being connected with the top end socket of the redistribution plate is
The impermeable structure of fluid, the part below the end of the impermeable structure of fluid can not for fluid-impermeable but solid catalyst
The open-celled structure of transmission；The perforate of the side wall is highly opened not less than the perforate height of central tube, the gas redistribution plate
Hole is highly not higher than the perforate height of central tube；The quantity of the gas redistribution plate is 1-50.
Preferably, also include being used for the catalysis of axial even partition in the receiving space of the Axial and radial catalytic reaction zone
The dividing plate of agent bed, the side both ends of the dividing plate are individually fixed on the tube wall of the side wall and the central tube, it is described every
The quantity of plate is 2-32.
Preferably, the back cover is spherical back cover.
Preferably, the top end socket is one kind in dome head, ellipsoidal head and flat-plate closure.
Preferably, the top end socket is the structure with the removable shifting of the side wall in order to the handling of catalyst.
Preferably, the reactor also includes unloading agent pipe for removal catalyst, and one end sealing for unloading agent pipe connects
Be connected to the back cover of Axial and radial catalytic reaction zone and with the internal fluid communication of the Axial and radial catalytic reaction zone, unload agent pipe
The other end seals the outside for reaching the housing.
Preferably, the reactor also include for removal catalyst unload agent pipe and for suction out catalyst unload agent dress
Put, described one end for unloading agent pipe be sealedly attached to the back cover of Axial and radial catalytic reaction zone and with the Axial and radial catalytic reaction
The internal fluid communication in area, the other end sealing for unloading agent pipe reach the outside of the housing, and the agent pipe that unloads has catalyst
Discharge port, the agent device that unloads are connected with the catalyst discharge port.
Preferably, the bottom of the air inlet pipe is provided with least one reaction gas for being used to be distributed the feeding reactor
Gas distributor.
Compared with prior art, the present invention has advantages below：
1st, reaction zone is made up of radial direction reaction zone and Axial response area, and catalytic reaction zone bottom is hemispherical, reacting gas
Beds can also be improved from side wall radially into beds from bottom axially into beds
Utilization rate；
2nd, gas redistribution plate and dividing plate are provided with bed, beds can be divided into multiple reaction zones, carried
The high uniformity of the fluid in beds, avoids reaction dead zone and gas Biased flow phenomenon occurs, the temperature of bed compared with
Be not in focus to be uniform, fully ensured that the even running in the whole service cycle.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of structural representation of embodiment of reactor provided by the invention；
Fig. 2 is a kind of sectional view (the i.e. section view in A-A faces in Fig. 1 of embodiment of reactor provided by the invention
Figure)；
Fig. 3 is the structural representation of another embodiment of reactor provided by the invention；
Fig. 4 is that (i.e. A-A faces cuts open in Fig. 3 for the sectional view of another embodiment of reactor provided by the invention
View)；
Fig. 5 is the structural representation of the third embodiment of reactor provided by the invention；
Fig. 6 is that (i.e. A-A faces cuts open in Fig. 5 for the sectional view of the third embodiment of reactor provided by the invention
View).
Description of reference numerals
The first gas distributor of 1 air inlet, 2 housing 3
The tube wall of 4 second gas distributor, 5 top end socket 6
The catalyst discharge port of 7 gases redistribution plate, 8 Axial and radial catalytic reaction zone 9
10 unload the annular space of 11 side wall of agent pipe 12
The gas outlet of 13 central tube, 14 escape pipe 15
The back cover of 16 air inlet pipe, 17 dividing plate 18
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of multi-bed layer shaft radial reactor, the reactor include radial direction cylindrical shape seal and pressure bearing housing 2,
From the top of the housing 2 extend into the air inlet pipe 16 of enclosure interior, be arranged on the lower section of air inlet pipe 16 in the housing 2 with
The coaxial Axial and radial catalytic reaction zone 8 of housing 2 and escape pipe 14；The Axial and radial catalytic reaction zone 8 is can containing catalyst
The cylindrical shape receiving space of bed, the shell of the receiving space is formed by side wall 11, top end socket 5 and back cover 18, wherein described
Side wall 11 and the selectively back cover 18 are fluid-impermeable but the impermeable open-celled structure of solid catalyst, the top
Portion's end socket 5 is the impermeable structure of fluid；One end of the escape pipe 14 is sealedly attached to the described of Axial and radial catalytic reaction zone 8
Top end socket 5 and with the internal fluid communication of the Axial and radial catalytic reaction zone 8, escape pipe 14 the other end sealing reaches institute
State the outside of housing 2；Formed with annular space between the side wall 11 of the Axial and radial catalytic reaction zone 8 and the madial wall of the housing 2
12, the air inlet pipe 16 is in fluid communication with the annular space 12.
According to the present invention, the Axial and radial catalytic reaction zone 8 has central tube 13, the central tube 13 and the escape pipe
14 are tightly connected and are in fluid communication, and the end being connected with the top end socket 5 of the central tube 13 is the impermeable knot of fluid
Structure, part below the end of the impermeable structure of fluid of central tube 13 for fluid-impermeable but solid catalyst it is impermeable
Open-celled structure.After reaction mass is entered in housing 2 by air inlet pipe 16, by annular space 12 radial through with open-celled structure
Side wall 11, or enter in Axial and radial catalytic reaction zone 8 and reacted axially through the back cover 18 with open-celled structure, in
Heart pipe 13 collects, and final reacting product leaves reactor from escape pipe 14.
It is described in order to further improve reaction mass being uniformly distributed in Axial and radial catalytic reaction zone 8 according to the present invention
Also include with housing 2 coaxial and with the receiving space the shell in the receiving space of Axial and radial catalytic reaction zone 8
The side wall 11 and back cover 18 at least one cylindrical gas redistribution plate 7 for matching of shape, gas redistribution
The end sealing of plate 7 is fixed on the top end socket 5；The shell of the receiving space and the outermost gas are again
Between distribution grid 7, between adjacent two gas redistribution plate 7 and the gas redistribution plate 7 of most inner side with it is described
Formed with catalyst bed sheaf space between central tube 13；The end being connected with the top end socket 5 of the redistribution plate 7 is stream
The impermeable structure of body, part below the end of the impermeable structure of fluid for fluid-impermeable but solid catalyst it is impermeable
The open-celled structure crossed.In order to avoid reaction dead zone and gas Biased flow phenomenon, the perforate of the side wall 11 is highly not less than central tube
13 perforate height, the perforate of the gas redistribution plate 7 is highly not higher than the perforate height of central tube 13.The gas divides again
The quantity of fabric swatch 7 can be adjusted according to the response situation of reality, such as can be 1-50.
It is described in order to further improve reaction mass being uniformly distributed in Axial and radial catalytic reaction zone 8 according to the present invention
The open-celled structure that central tube 13, side wall 11, back cover 18 and the gas of Axial and radial catalytic reaction zone 8 redistribute plate 7 can wrap
Include and be respectively arranged with size identical gas distribution holes on central tube 13, side wall 11, back cover 18 and gas redistribution plate 7.Need
It is noted that the gas distribution holes that those skilled in the art often say, can be square hole, slot, circular port, ellipse
The well formats such as shape hole, bellmouth.Central tube 13, side wall 11 can also use the Johnson Net for meeting mechanical strength, technological requirement.
It is described in order to further improve reaction mass being uniformly distributed in Axial and radial catalytic reaction zone 8 according to the present invention
Also include the dividing plate 17 for axial even partition beds, institute in the receiving space of Axial and radial catalytic reaction zone 8
The side both ends for stating dividing plate 17 are individually fixed on the tube wall 6 of the side wall 11 and the central tube 13.It is dead in order to avoid reacting
Area and gas Biased flow phenomenon, the height of the dividing plate between the perforate height and the perforate height of central tube 13 of side wall 11,
It is or highly identical with the perforate of central tube 13.The quantity of the dividing plate 17 can be adjusted according to the response situation of reality, example
It such as can be 2-32.
According to the present invention, the gas redistribution plate 7 and/or dividing plate 17 can use metal material, ceramic material, preferably
Using the metal material not reacted with the gas in reaction system.
According to the present invention, in order to improve the utilization rate of beds, the back cover 18 can be spherical back cover so that anti-
Answer gas can be from back cover 18 axially into Axial and radial catalytic reaction zone 8.
According to the present invention, the shape of the top end socket 5 does not have special limitation, for example, can be selected from dome head,
One kind in ellipsoidal head and flat-plate closure.
According to the present invention, for the ease of the handling of catalyst, the top end socket 5 is the knot with the 11 removable shifting of side wall
Structure.Such as when loading microspherical catalyst, the top end socket 5 can be torn open shifting, utilize the mode loading catalyst of pumping, catalysis
The top end socket 5 is installed as the state that is tightly connected with the side wall 11 again after the completion of agent filling；It is catalyzed when needing removal
During agent, the top end socket 5 can also be torn open and move and completed by unloading agent device.
According to a kind of embodiment of the present invention, it is unfavorable for when reactor size is larger by removing top end socket 5
When carrying out removal catalyst, the reactor also includes unloading agent pipe 10 for removal catalyst, it is described unload agent pipe 10 one end it is close
Envelope be connected to Axial and radial catalytic reaction zone 8 the back cover 18 and with the internal fluid communication of the Axial and radial catalytic reaction zone 8,
The other end sealing for unloading agent pipe 10 reaches the outside of the housing 2, and the agent pipe 10 that unloads has catalyst discharge port 9.Ability
Field technique personnel are it is understood that the part unloaded agent pipe 10 and be connected with the back cover 18 of Axial and radial catalytic reaction zone 8
The baffle plate of one piece of impermeable controllable switch of fluid is should be, when being reacted, the baffle plate is in closed mode, anti-to avoid
Answering material, the baffle plate is opened when needing to unload agent can be such that catalyst is drawn off by unloading agent pipe 10 from the outflow of agent pipe is unloaded.
According to a kind of embodiment of the present invention, plate 7 and/or dividing plate 17 are redistributed when gas in reactor be present
When, what the reactor also included being used for suctioning out catalyst unloads agent device, it is described unload agent device removably with the catalyst
Discharge port 9 is connected.It will be appreciated by persons skilled in the art that it is described unload agent device without all the time with the catalyst discharge port
9 are connected, and are only attached use when needing removal catalyst.The agent device that unloads is the device with strong suction, as long as can
To reach the purpose that catalyst is suctioned out to reactor, the present invention does not do special limitation, such as can be conventional dust catcher
Deng.
According to the present invention, the bottom of the air inlet pipe 16 can be provided with it is at least one be used to be distributed be sent into the reactor
Reaction gas gas distributor.The gas distributor can use those skilled in the art institute conventional use of, the present invention
Repeat no more, the gas distributor is preferably provided with two.
The present invention is further illustrated by embodiment below in conjunction with accompanying drawing, but therefore the present invention is not taken office
What is limited.
Embodiment 1
As shown in figure 1, used by the present embodiment multi-bed layer shaft radial reactor include cylindrical shape seal and pressure bearing housing 2,
The air inlet pipe 16 of enclosure interior is extend into from the top of housing 2, is arranged on the coaxial with housing 2 of the lower section of air inlet pipe 16 in housing 2
Axial and radial catalytic reaction zone 8 and escape pipe 14.The top of air inlet pipe 16 has air inlet 1, and bottom is distributed provided with first gas
Device 3, the lower section of first gas distributor 3 are provided with second gas distributor 4.Axial and radial catalytic reaction zone 8 is that can accommodate catalysis
The cylindrical shape receiving space of agent bed, the shell of the receiving space are formed by side wall 11, top end socket 5 and back cover 18, top envelope
First 5 be dome head, and side wall 11 and back cover 18 have open-celled structure, and back cover 18 is spherical back cover.Axial and radial catalytic reaction zone 8
With central tube 13, the part below the end being connected with top end socket 5 of central tube 13 is open-celled structure.Axial and radial catalysis is anti-
Answer and 12 pieces of dividing plates are axially evenly arranged with area 8, angle is 30 ° between adjacent separator；Also set up in Axial and radial catalytic reaction zone 8
There are 3 equidistant cylindrical gas redistribution plates, gas redistributes the portion below the end being connected with top end socket 5 of plate 7
It is divided into open-celled structure.Escape pipe 14 has gas outlet 15.The bottom of Axial and radial catalytic reaction zone 8, which is provided with, unloads agent pipe 10, unloads agent pipe
10 have catalyst discharge port 9.Formed with annular space 12 between the side wall 11 of Axial and radial catalytic reaction zone 8 and the madial wall of housing 2.
The internal diameter of reactor shell 2 is 1200mm, and the spacing of annular space 12 is 50mm, and the internal diameter of central tube 6 is 200mm, Axial and radial
The catalyst bed layer height of reaction zone 8 is 1600mm, and 3 gas redistribution plates 17 are equally arranged at Axial and radial catalytic reaction
In the receiving space in area 8, gas redistribution plate 7 and side wall 11 between, adjacent gas redistribution plate 7 between and gas redistribute
The distance between tube wall 6 of plate 7 and central tube 13 is 225mm.Side wall 11, gas redistribution plate 7, central tube 13 are circle
Perforate, percent opening are respectively 1.0%, 2.5%, 3.0%.Hang down the perforate height distance Axial and radial catalytic reaction zone bottom of side wall 11
Straight height is 1500mm；Gas redistributes plate 7 and the perforate of perforate center tube wall 6 is highly identical, with Axial and radial catalytic reaction zone
Bottom vertical height is 1450mm.The height of dividing plate and Axial and radial catalytic reaction zone bottom vertical height are 1550mm.
The reactor of the present embodiment is applied to synthesis gas methanation reaction, synthesis gas enters reactor from air inlet 1, and one
Part by side wall 11 radially across catalytic reaction zone, a part by back cover 18 axially across catalytic reaction zone after, in central tube 13
In collect, from gas outlet 15 discharge reactor.Feed composition molal volume fraction is H2：39.9%th, CO：8.7%th, CO2：
4.3%th, H2O：17.3%th, CH4：29.8%, reaction feed temperature is 280 DEG C, feed pressure 3.2MPa, and feed rate is
1500kmol/h。
From the point of view of the Temperature Distribution of beds, bed hotspot location is 250mm apart from the average distance of side wall 11, heat
Point value is 923K.What is provided in table 1 is the multi-bed layer shaft radial reactor and radial reactor pair in the prior art of the present embodiment
The situation of ratio.It should be noted that two kinds of reactor catalyst loadings are identical.From the bed uniformity, hotspot location, CO conversion ratios
The reactor that three indexs can be seen that the present embodiment shows more excellent performance.
The multi-bed layer shaft radial reactor that the present embodiment of table 1 uses contrasts with conventional radial reactor
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratios/(%) |
| Conventional radial reactor | 0.90 | 265 | 65 |
| The reactor of the present embodiment | 0.96 | 250 | 74 |
Embodiment 2
As shown in Figure 3, Figure 4, the reactor shell internal diameter of the present embodiment reactor and embodiment 1, catalytic reaction zone height,
The structural parameters such as perforate are identical.It is with the difference of embodiment 1, dividing plate is not provided with the reactor of the present embodiment.This reality
The reactor for applying example can be equally used for methanation reaction.It is identical with the process conditions that embodiment 1 uses.
From the point of view of the Temperature Distribution of beds, bed hotspot location is 255mm apart from the average distance of side wall 11, heat
Point value is 923K.What is provided in table 2 is the multi-bed layer shaft radial reactor and radial reactor pair in the prior art of the present embodiment
The situation of ratio.Equally, two kinds of reactor catalyst loadings are identical.From three the bed uniformity, hotspot location, CO conversion ratios indexs
As can be seen that reactor proposed by the present invention shows more excellent performance.
More bed radial reactors that the present embodiment of table 2 uses contrast with conventional radial reactor
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratios/(%) |
| Conventional radial reactor | 0.90 | 265 | 65 |
| The reactor of the present embodiment | 0.95 | 255 | 73 |
Embodiment 3
As shown in Figure 5, Figure 6, the reactor shell internal diameter of the present embodiment reactor and embodiment 1, catalytic reaction zone height,
The structural parameters such as perforate are identical.It is with the difference of embodiment 1, gas redistribution is not provided with the reactor of the present embodiment
Plate, and the quantity of dividing plate is 9, the angle between adjacent separator is 40 °.The reactor of the present embodiment can be equally used for methane
Change reaction.It is identical with the process conditions that embodiment 1 uses.
From the point of view of the Temperature Distribution of beds, bed hotspot location is 257mm apart from the average distance of side wall 11, heat
Point value is 923K.What is provided in table 3 is the multi-bed layer shaft radial reactor and radially reaction in the prior art that the present embodiment uses
Device contrasts situation.Equally, two kinds of reactor catalyst loadings are identical.From the bed uniformity, hotspot location, CO conversion ratios three
Index can be seen that reactor proposed by the present invention and show more excellent performance.
More bed radial reactors that the present embodiment of table 3 uses contrast with conventional radial reactor
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratios/(%) |
| Conventional radial reactor | 0.90 | 265 | 65 |
| The reactor of the present embodiment | 0.93 | 257 | 71 |
Radial reactor provided by the invention is compact-sized, even fluid distribution degree is higher, bed space availability ratio is high, nothing
Fluid bias current and short circuit phenomenon.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of multi-bed layer shaft radial reactor, it is characterised in that the reactor includes radial direction cylindrical shape seal and pressure bearing housing
(2), it extend into the air inlet pipe (16) of enclosure interior at the top of the housing (2), is arranged on the air inlet pipe in the housing (2)
(16) the Axial and radial catalytic reaction zone (8) coaxial with housing (2) and escape pipe (14) below；The Axial and radial catalysis is anti-
Answer area (8) for can containing catalyst bed cylindrical shape receiving space, the shell of the receiving space is by side wall (11), top end socket
(5) formed with back cover (18), wherein the side wall (11) and the selectively back cover (18) are fluid-impermeable but solid
The impermeable open-celled structure of catalyst, the top end socket (5) are the impermeable structure of fluid；The one of the escape pipe (14)
End be sealedly attached to Axial and radial catalytic reaction zone (8) the top end socket (5) and with the Axial and radial catalytic reaction zone (8)
Internal fluid communication, the other end sealing of escape pipe (14) reach the outside of the housing (2)；The Axial and radial catalytic reaction
Formed with annular space (12), the air inlet pipe (16) and the ring between the side wall (11) in area (8) and the madial wall of the housing (2)
Gap (12) is in fluid communication.
2. reactor according to claim 1, wherein, the Axial and radial catalytic reaction zone (8) has central tube (13), in described
Heart pipe (13) and the escape pipe (14) are tightly connected and are in fluid communication, the central tube (13) with the top end socket (5)
The end of connection is the impermeable structure of fluid, and the part below the end of the impermeable structure of fluid of central tube (13) is stream
The open-celled structure that body can pass through but solid catalyst is impermeable.
3. reactor according to claim 2, wherein, also wrapped in the receiving space of the Axial and radial catalytic reaction zone (8)
Include the side wall (11) of the shell coaxial with housing (2) and with the receiving space and the shape of back cover (18) matches
At least one cylindrical gas redistribution plate (7), the end sealing of gas redistribution plate (7) is fixed on the top envelope
On head (5)；Between the shell of the receiving space and outermost gas redistribution plate (7), it is adjacent two described in
Between gas redistribution plate (7) and between the gas redistribution plate (7) and the central tube (13) of most inner side formed with
Catalyst bed sheaf space；The end being connected with the top end socket (5) of the gas redistribution plate (7) is impermeable for fluid
Structure, part below the end of the impermeable structure of fluid are fluid-impermeable but the impermeable perforate knot of solid catalyst
Structure；The perforate of the side wall (11) is highly not less than the perforate height of central tube (13), the perforate of the gas redistribution plate (7)
Highly not higher than the perforate height of central tube (13)；The quantity of the gas redistribution plate (7) is 1-50.
4. reactor according to claim 2, wherein, also wrapped in the receiving space of the Axial and radial catalytic reaction zone (8)
The dividing plate (17) for axial even partition beds is included, the side both ends of the dividing plate (17) are individually fixed in the side
On the tube wall (6) of wall (11) and the central tube (13), the quantity of the dividing plate (17) is 2-32.
5. reactor according to claim 1, wherein, the back cover (18) is spherical back cover.
6. reactor according to claim 1, wherein, the top end socket (5) is selected from dome head, ellipsoidal head peace
One kind in plate end socket.
7. reactor according to claim 1, wherein, the top end socket (5) is the structure with the side wall (11) removable shifting
In order to the handling of catalyst.
8. reactor according to claim 1, wherein, the reactor also includes unloading agent pipe (10) for removal catalyst,
Described one end for unloading agent pipe (10) be sealedly attached to the back cover (18) of Axial and radial catalytic reaction zone (8) and with the Axial and radial
The internal fluid communication of catalytic reaction zone (8), the other end sealing for unloading agent pipe (10) reach the outside of the housing (2).
9. according to the reactor of claim 3 or 4, wherein, the reactor also includes unloading agent pipe for removal catalyst
(10) agent device and for suction out catalyst is unloaded, described one end for unloading agent pipe (10) is sealedly attached to Axial and radial catalytic reaction zone
(8) the back cover (18) and with the internal fluid communication of the Axial and radial catalytic reaction zone (8), unload the other ends of agent pipe (10)
Sealing reaches the outsides of the housing (2), and the agent pipe (10) that unloads has a catalyst discharge port (9), it is described unload agent device and
The catalyst discharge port (9) is connected.
10. reactor according to claim 1, wherein, the bottom of the air inlet pipe (16), which is provided with, at least one to be used to be distributed
It is sent into the gas distributor of the reaction gas of the reactor.
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| CN201610454666.3A CN107519822B (en) | 2016-06-21 | 2016-06-21 | A kind of multi-bed layer shaft radial reactor |
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| CN201610454666.3A CN107519822B (en) | 2016-06-21 | 2016-06-21 | A kind of multi-bed layer shaft radial reactor |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4372920A (en) * | 1979-07-13 | 1983-02-08 | Ammonia Casale S.A. | Axial-radial reactor for heterogeneous synthesis |
| CN203108514U (en) * | 2013-01-15 | 2013-08-07 | 中国石化工程建设有限公司 | Axial and radial fixed bed methanation reactor |
| CN203108515U (en) * | 2013-03-18 | 2013-08-07 | 青岛联信催化材料有限公司 | Reactor for shift reaction |
| CN203123947U (en) * | 2013-02-07 | 2013-08-14 | 中石化宁波工程有限公司 | Axial-radial reactor structure for sulfur-resisting conversion process |
| CN204412216U (en) * | 2014-12-26 | 2015-06-24 | 中国天辰工程有限公司 | A kind of Axial and radial gas solid reactor |
-
2016
- 2016-06-21 CN CN201610454666.3A patent/CN107519822B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4372920A (en) * | 1979-07-13 | 1983-02-08 | Ammonia Casale S.A. | Axial-radial reactor for heterogeneous synthesis |
| CN203108514U (en) * | 2013-01-15 | 2013-08-07 | 中国石化工程建设有限公司 | Axial and radial fixed bed methanation reactor |
| CN203123947U (en) * | 2013-02-07 | 2013-08-14 | 中石化宁波工程有限公司 | Axial-radial reactor structure for sulfur-resisting conversion process |
| CN203108515U (en) * | 2013-03-18 | 2013-08-07 | 青岛联信催化材料有限公司 | Reactor for shift reaction |
| CN204412216U (en) * | 2014-12-26 | 2015-06-24 | 中国天辰工程有限公司 | A kind of Axial and radial gas solid reactor |
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| CN107519822B (en) | 2019-05-10 |
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