CN107519822B - 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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- CN107519822B CN107519822B CN201610454666.3A CN201610454666A CN107519822B CN 107519822 B CN107519822 B CN 107519822B CN 201610454666 A CN201610454666 A CN 201610454666A CN 107519822 B CN107519822 B CN 107519822B
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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
Abstract
The invention discloses a kind of multi-bed layer shaft radial reactor, which includes radial cylinder-shaped seal and pressure bearing shell (2), air inlet pipe (16), axis radial direction catalytic reaction zone (8) and escape pipe (14)；Axis radial direction catalytic reaction zone (8) be can containing catalyst bed cylinder-shaped accommodation space, the shell of the accommodation space is formed by side wall (11), top end socket (5) and back cover (18), the wherein side wall (11) the and selectively back cover (18) is fluid-impermeable but the impermeable open-celled structure of solid catalyst, the top end socket (5) is the impermeable structure of fluid.The reactor pressure decrease is low, space utilization rate 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 reactors.
Background technique
There are mainly of two types for fixed bed reactors, and one is axially-located bed reactor, another kind is radial fixed-bed
Reactor.Axially-located bed reactor design, process are relatively easy, easy to operate, but there are reactor apparatus size Pangs
Greatly, bed pressure drop is big, is easy to appear local run aways, moves the problems such as heat is slow, conversion ratio is low, enlarge-effect is obvious.Radial bed is anti-
Answer device have ratio of height to diameter is larger, bed pressure drop is small, reactant the catalyst bed 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 enlargement, but difficult to realize reactant is in the radial direction is uniformly distributed.
The superiority and inferiority of radial bed reactor design is affected to reaction process.It is real that fluid is axially evenly distributed with problem in bed
The key problem in technology of existing such reactor optimization design.Reactant distribution uniformly whether, be directly related to reactant conversion ratio, produce
The selectivity of object and the operational stability of reactor.Zhang Chengfang et al. (research (II) of radial reactor uniform fluid distribution design
[J] chemical engineering, 1980,2 (2): 82-89.), Wang Jinfu et al. (reform the fluid force scholarship and moral conduct of radial reactor gas distribution system
For and its optimization design [J] petroleum refining and chemical industry, 1997,28 (4): 47-52.) propose radial reactor uniform fluid distribution
Method.In general, uniform fluid distribution is mainly to pass through to choose the side that runner, mass flow pathway form and percent opening appropriate control
Method realization is evenly distributed with fluid.
Therefore, in order to further increase the fluid uniformity of radial reactor, meet radial reactor constantly enlargement
Growth requirement is still a technical problem to be solved urgently, while being also the developing direction of the following radial fixed-bed reactor.
Summary of the invention
The object of the present invention is to provide a kind of multi-bed layer shaft radial reactor, the reactor pressure decrease is low, space utilization rate is high,
Without gas bias current and short circuit phenomenon.
To achieve the goals above, the present invention provides a kind of multi-bed layer shaft radial reactor, which includes radial circle
Shaped seals pressure-bearing shell, the air inlet pipe that enclosure interior is extend into from the case top, be arranged in the shell it is described into
The axis radial direction catalytic reaction zone and escape pipe coaxial with shell below tracheae；Axis radial direction catalytic reaction zone is that can hold
Receive the cylinder-shaped accommodation space of catalyst bed, the shell of the accommodation space is formed by side wall, top end socket and back cover, wherein institute
It states 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 axis radial direction catalytic reaction zone
Head and the internal fluid communication with axis radial direction catalytic reaction zone, the other end sealing of escape pipe reach the outer of the shell
Portion；Annular space, the air inlet pipe and institute are formed between the side wall of axis radial direction catalytic reaction zone and the inner sidewall of the shell
State annular fluid connection.
Preferably, axis radial direction catalytic reaction zone has central tube, and the central tube and the escape pipe are tightly connected
And be in fluid communication, the end of the central tube connecting with the top end socket is the impermeable structure of fluid, the stream of central tube
The end part below of the impermeable structure of body is fluid-impermeable but the impermeable open-celled structure of solid catalyst.
Preferably, further include in the accommodation space of axis radial direction catalytic reaction zone it is coaxial with shell and with the appearance
Receive the side wall of the shell and at least one cylindrical gas that the shape of back cover matches redistribution plate in space, it is described
The end sealing of gas redistribution plate is fixed on the top end socket；The shell of the accommodation space and outermost institute
It states between gas redistribution plate, adjacent two gas redistributes between plate and the innermost gas redistribution plate
Catalyst bed sheaf space is formed between the central tube；The end of the redistribution plate connecting with the top end socket is
The end part below of the impermeable structure of fluid, the impermeable structure of fluid is fluid-impermeable but solid catalyst can not
The open-celled structure of transmission；The aperture height of the side wall is not less than the aperture height of central tube, and the gas redistribution plate is opened
Hole height is not higher than the aperture height of central tube；The quantity of the gas redistribution plate is 1-50.
It preferably, further include for axial even partition catalysis in the accommodation space of axis radial direction catalytic reaction zone
The side both ends of the partition of agent bed, the partition 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 selected from one of dome head, ellipsoidal head and flat-plate closure.
Preferably, the top end socket is the handling with the structure of the removable shifting of the side wall in order to catalyst.
Preferably, the reactor further includes unloading agent pipe for removal catalyst, and one end sealing for unloading agent pipe connects
It is connected to the back cover of axis radial direction catalytic reaction zone and the internal fluid communication with axis radial direction catalytic reaction zone, unloads agent pipe
The other end seals the outside for reaching the shell.
Preferably, the reactor further include for removal catalyst unload agent pipe and for be sucked out catalyst unload agent dress
It sets, described one end for unloading agent pipe is sealedly attached to the back cover of axis radial direction catalytic reaction zone and radially catalysis is reacted with the axis
The internal fluid communication in area, the other end sealing for unloading agent pipe reach the outside of the shell, and the agent pipe that unloads is with catalyst
Discharge port, the agent device that unloads are connected with the catalyst discharge port.
Preferably, the lower part of the air inlet pipe is provided at least one for being distributed the reaction gas for being sent into the reactor
Gas distributor.
Compared with prior art, the invention has the following advantages that
1, reaction zone is made of radial reaction zone and Axial response area, and catalytic reaction zone bottom is hemispherical, reaction gas
Catalyst bed can also be improved from bottom axially into catalyst bed from side wall radially into catalyst bed
Utilization rate；
2, it is provided with gas redistribution plate and partition in bed, catalyst bed can be divided into multiple reaction zones, mentioned
The high uniformity of the fluid in catalyst bed, avoids reaction dead zone and gas Biased flow phenomenon occurs, the temperature of bed compared with
It is uniform, is not in hot spot, has fully ensured that the even running in the whole service period.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, 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 schematic diagram of specific embodiment of reactor provided by the invention；
Fig. 2 is a kind of cross-sectional view (the i.e. section view in the face A-A in Fig. 1 of specific embodiment of reactor provided by the invention
Figure)；
Fig. 3 is the structural schematic diagram of another specific embodiment of reactor provided by the invention；
Fig. 4 is that (i.e. the face A-A cuts open in Fig. 3 for the cross-sectional view of another specific embodiment of reactor provided by the invention
View)；
Fig. 5 is the structural schematic diagram of the third specific embodiment of reactor provided by the invention；
Fig. 6 is that (i.e. the face A-A cuts open in Fig. 5 for the cross-sectional view of the third specific embodiment of reactor provided by the invention
View).
Description of symbols
1 air inlet, 2 shell, 3 first gas distributor
4 second gas distributor, 5 top end socket, 6 tube wall
7 gases redistribute 8 axis radial direction catalytic reaction zone of plate, 9 catalyst discharge port
10 unload 11 side wall of agent pipe, 12 annular space
13 central tube, 14 escape pipe, 15 gas outlet
16 air inlet pipe, 17 partition, 18 back cover
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched
The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of multi-bed layer shaft radial reactor, the reactor include radial cylinder-shaped seal and pressure bearing shell 2,
The air inlet pipe 16 of enclosure interior is extend at the top of the shell 2, be arranged in the shell 2 below the air inlet pipe 16 with
The coaxial axis radial direction catalytic reaction zone 8 of shell 2 and escape pipe 14；Axis radial direction catalytic reaction zone 8 is can containing catalyst
The shell of the cylinder-shaped accommodation space of bed, the accommodation 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 axis radial direction catalytic reaction zone 8
The other end sealing of top end socket 5 and the internal fluid communication with axis radial direction catalytic reaction zone 8, escape pipe 14 reaches institute
State the outside of shell 2；Annular space is formed between the side wall 11 of axis radial direction catalytic reaction zone 8 and the inner sidewall of the shell 2
12, the air inlet pipe 16 is in fluid communication with the annular space 12.
According to the present invention, axis radial direction 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 of the central tube 13 connecting with the top end socket 5 is the impermeable knot of fluid
The end part below of structure, the impermeable structure of the fluid of central tube 13 is fluid-impermeable but solid catalyst is impermeable
Open-celled structure.After reaction mass is entered in shell 2 by air inlet pipe 16, by annular space 12 radial through with open-celled structure
Side wall 11, or enter in axis radial direction 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.
According to the present invention, described in order to further increase reaction mass being uniformly distributed in axis radial direction catalytic reaction zone 8
It further include the shell coaxial with shell 2 and with the accommodation space in the accommodation space of axis radial direction 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 accommodation space and the outermost gas are again
Between distribution grid 7, between adjacent two gas redistribution plate 7 and the innermost gas redistribution plate 7 with it is described
Catalyst bed sheaf space is formed between central tube 13；The end of the redistribution plate 7 connecting with the top end socket 5 is stream
The end part below of the impermeable structure of body, the impermeable structure of fluid is fluid-impermeable but solid catalyst is impermeable
The open-celled structure crossed.In order to avoid reaction dead zone and gas Biased flow phenomenon, the aperture height of the side wall 11 is not less than central tube
The aperture height of 13 aperture height, the gas redistribution plate 7 is not higher than the aperture height of central tube 13.The gas divides again
The quantity of fabric swatch 7 can be adjusted according to actual response situation, such as can be 1-50.
According to the present invention, described in order to further increase reaction mass being uniformly distributed in axis radial direction catalytic reaction zone 8
The open-celled structure that central tube 13, side wall 11, back cover 18 and the gas of axis radial direction catalytic reaction zone 8 redistribute plate 7 can wrap
It includes and is respectively arranged with the identical gas distribution holes of size on central tube 13, side wall 11, back cover 18 and gas redistribution plate 7.It needs
It is noted that the gas distribution holes that those skilled in the art often say, can be square hole, slot, round hole, ellipse
The well formats such as shape hole, bellmouth.The Johnson Net for meeting mechanical strength, technique requirement also can be used in central tube 13, side wall 11.
According to the present invention, described in order to further increase reaction mass being uniformly distributed in axis radial direction catalytic reaction zone 8
It further include the partition 17 for axial even partition catalyst bed, institute in the accommodation space of axis radial direction catalytic reaction zone 8
The side both ends for stating partition 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 partition between the aperture height of side wall 11 and the aperture height of central tube 13,
Or it is identical as the aperture height of central tube 13.The quantity of the partition 17 can be adjusted according to actual response situation, example
It can be such as 2-32.
According to the present invention, the gas redistribution plate 7 and/or partition 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 catalyst bed, the back cover 18 can be spherical back cover, so that instead
Answer gas can be from back cover 18 axially into axis radial direction catalytic reaction zone 8.
According to the present invention, the shape of the top end socket 5 does not have a special limitation, for example, can for selected from dome head,
One of 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 removable shifting of the side wall 11
Structure.Such as when loading microspherical catalyst, the top end socket 5 can be torn open shifting, the loading catalyst in the way of pumping, catalysis
The top end socket 5 is installed as the state being tightly connected with the side wall 11 again after the completion of agent filling；When needing removal to be catalyzed
When agent, the top end socket 5 can also be torn open and move and completed by unloading agent device.
A kind of specific embodiment according to the present invention is unfavorable for when reactor size is larger by removing top end socket 5
When carrying out removal catalyst, the reactor further includes unloading agent pipe 10 for removal catalyst, and described one end for unloading agent pipe 10 is close
Envelope be connected to axis radial direction catalytic reaction zone 8 the back cover 18 and the internal fluid communication with axis radial direction catalytic reaction zone 8,
The other end sealing for unloading agent pipe 10 reaches the outside of the shell 2, and the agent pipe 10 that unloads is with catalyst discharge port 9.Ability
Field technique personnel are it is understood that the part unloading agent pipe 10 and connecting with the back cover 18 of axis radial direction catalytic reaction zone 8
The baffle that should be one piece of impermeable controllable switch of fluid, when being reacted, the baffle is in closed state, to avoid anti-
Answer material from the outflow of agent pipe is unloaded, the baffle is opened when needing to unload agent can be such that catalyst is drawn off by unloading agent pipe 10.
A kind of specific embodiment according to the present invention, when there are gas redistribution plate 7 and/or partitions 17 in reactor
When, the reactor further includes unloading agent device for be sucked out catalyst, 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 always with the catalyst discharge port
9 are connected, and use is only attached when needing removal catalyst.The agent device that unloads is the device with strong suction, as long as can
To achieve the purpose that for catalyst to be sucked out reactor, the present invention does not do special limitation, such as can be conventional dust catcher
Deng.
According to the present invention, the lower part of the air inlet pipe 16 can be set at least one for be distributed the feeding reactor
Reaction gas gas distributor.The gas distributor can be conventional use of using those skilled in the art institute, the present invention
It repeats no more, there are two the gas distributor is preferably provided with.
The present invention is further illustrated by embodiment below in conjunction with attached drawing, but therefore the present invention is not taken office
What is limited.
Embodiment 1
As shown in Figure 1, multi-bed layer shaft radial reactor used by the present embodiment include cylinder-shaped seal and pressure bearing shell 2,
Extend at the top of shell 2 air inlet pipe 16 of enclosure interior, be arranged in shell 2 it is coaxial with shell 2 below air inlet pipe 16
Axis radial direction catalytic reaction zone 8 and escape pipe 14.The top of air inlet pipe 16 has air inlet 1, and lower part is distributed equipped with first gas
Device 3, the lower section of first gas distributor 3 are provided with second gas distributor 4.Axis radial direction catalytic reaction zone 8 is that can accommodate catalysis
The shell of the cylinder-shaped accommodation space of agent bed, the accommodation space is 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.Axis radial direction catalytic reaction zone 8
With central tube 13, the end part below of central tube 13 connecting with top end socket 5 is open-celled structure.Radially catalysis is anti-for axis
It answers and is axially evenly arranged with 12 pieces of partitions in area 8, angle is 30 ° between adjacent separator；It is also set up in axis radial direction catalytic reaction zone 8
There are 3 equidistant cylindrical gas redistribution plates, gas redistributes the end portion below of plate 7 connecting with top end socket 5
It is divided into open-celled structure.Escape pipe 14 has gas outlet 15.8 bottom of axis radial direction catalytic reaction zone, which is provided with, unloads agent pipe 10, unloads agent pipe
10 have catalyst discharge port 9.Annular space 12 is formed between the side wall 11 of axis radial direction catalytic reaction zone 8 and the inner sidewall of shell 2.
2 internal diameter of reactor shell is 1200mm, and 12 spacing of annular space is 50mm, and 6 internal diameter of central tube is 200mm, and axis is radial
The catalyst bed layer height of reaction zone 8 is 1600mm, and 3 gas redistribution plates 17 are equally set to axis radially catalysis reaction
In the accommodation space in area 8, gas is redistributed between plate 7 and side wall 11, adjacent gas redistributes between plate 7 and gas redistributes
The distance between the tube wall 6 of plate 7 and central tube 13 is 225mm.Side wall 11, gas redistribution plate 7, central tube 13 are circle
Aperture, percent opening are respectively 1.0%, 2.5%, 3.0%.It hangs down the aperture height distance axis radial direction catalytic reaction zone bottom of side wall 11
Straight height is 1500mm；Gas redistributes plate 7 and the aperture height of aperture center tube wall 6 is identical, with axis radial direction catalytic reaction zone
Bottom vertical height is 1450mm.The height and axis radial direction catalytic reaction zone bottom vertical height of partition are 1550mm.
By the reactor of the present embodiment be applied to synthesis gas methanation reaction, synthesis gas from air inlet 1 enter reactor, 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 be discharged reactor.Feed composition molal volume score is H2: 39.9%, CO:8.7%, CO2:
4.3%, H2O:17.3%, 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 catalyst bed, average distance of the bed hotspot location apart from side wall 11 is 250mm, 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
Compare situation.It should be noted that two kinds of reactor catalyst loadings are identical.From the bed uniformity, hotspot location, CO conversion ratio
The reactor that three indexs can be seen that the present embodiment shows more excellent performance.
The multi-bed layer shaft radial reactor and conventional radial reactor that 1 the present embodiment of table uses compare
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratio/(%) |
| 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 aperture are identical.Difference from example 1 is that being not provided with partition in the reactor of the present embodiment.This reality
The reactor for applying example can be equally used for methanation reaction.It is identical as the process conditions that embodiment 1 uses.
From the point of view of the Temperature Distribution of catalyst bed, average distance of the bed hotspot location apart from side wall 11 is 255mm, 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
Compare situation.Equally, two kinds of reactor catalyst loadings are identical.From three the bed uniformity, hotspot location, CO conversion ratio indexs
As can be seen that reactor proposed by the present invention shows more excellent performance.
The more bed radial reactors and conventional radial reactor that 2 the present embodiment of table uses compare
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratio/(%) |
| 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 aperture are identical.Difference from example 1 is that being not provided with gas redistribution in the reactor of the present embodiment
Plate, and the quantity of partition 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 as the process conditions that embodiment 1 uses.
From the point of view of the Temperature Distribution of catalyst bed, average distance of the bed hotspot location apart from side wall 11 is 257mm, heat
Point value is 923K.What is provided in table 3 is that the multi-bed layer shaft radial reactor that the present embodiment uses is reacted with radial in the prior art
Device comparative situation.Equally, two kinds of reactor catalyst loadings are identical.From the bed uniformity, hotspot location, CO conversion ratio three
Index can be seen that reactor proposed by the present invention and show more excellent performance.
The more bed radial reactors and conventional radial reactor that 3 the present embodiment of table uses compare
| Type of reactor | The uniformity | Hotspot location/(mm) | CO conversion ratio/(%) |
| 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 utilization rate is high, nothing
Fluid bias current and short circuit phenomenon.
It is described the prefered embodiments of the present invention in detail above in conjunction with attached drawing, still, the present invention is not limited to above-mentioned realities
The detail in mode is applied, within the scope of the technical concept of the present invention, a variety of letters can be carried out to technical solution of the present invention
Monotropic type, these simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
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 also be regarded as the disclosure of the present invention.
Claims (10)
1. a kind of multi-bed layer shaft radial reactor, which is characterized in that the reactor includes radial cylinder-shaped seal and pressure bearing shell
(2), it extend into the air inlet pipe (16) of enclosure interior at the top of the shell (2), the air inlet pipe is set in the shell (2)
(16) the axis radial direction catalytic reaction zone (8) and escape pipe (14) coaxial with shell (2) below；Radially catalysis is anti-for the axis
Answer area (8) be can containing catalyst bed cylinder-shaped accommodation space, the shell of the accommodation space is by side wall (11), top end socket
(5) it is 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 axis radial direction catalytic reaction zone (8) the top end socket (5) and with axis radial direction catalytic reaction zone (8)
Internal fluid communication, the other end sealing of escape pipe (14) reach the outside of the shell (2)；The axis radially catalysis reaction
It is formed with annular space (12) between the side wall (11) in area (8) and the inner sidewall of the shell (2), the air inlet pipe (16) and the ring
Gap (12) is in fluid communication.
2. reactor according to claim 1, wherein axis radial direction catalytic reaction zone (8) have central tube (13), it is described in
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 end part below 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 accommodation space of axis radial direction catalytic reaction zone (8)
The shape of the side wall (11) and back cover (18) that include the shell coaxial with shell (2) and with the accommodation space matches
At least one cylindrical gas redistribute plate (7), the end sealing of gas redistribution plate (7) is fixed on the top envelope
On head (5)；Between the shell of the accommodation space and outermost gas redistribution plate (7), it is two adjacent described in
It is formed between gas redistribution plate (7) and between innermost gas redistribution plate (7) and the central tube (13)
Catalyst bed sheaf space；The end of gas redistribution plate (7) connecting with the top end socket (5) is that fluid is impermeable
Structure, the end part below of the impermeable structure of fluid are fluid-impermeable but the impermeable aperture knot of solid catalyst
Structure；The aperture height of the side wall (11) is not less than the aperture height of central tube (13), the aperture of gas redistribution plate (7)
Height is not higher than the aperture height of central tube (13)；The quantity of gas redistribution plate (7) is 1-50.
4. reactor according to claim 2, wherein also wrapped in the accommodation space of axis radial direction catalytic reaction zone (8)
The partition (17) for axial even partition catalyst bed is included, the side both ends of the partition (17) are individually fixed in the side
On the tube wall (6) of wall (11) and the central tube (13), the quantity of the partition (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 of 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 further includes unloading agent pipe (10) for removal catalyst,
Described one end for unloading agent pipe (10) is sealedly attached to the back cover (18) of axis radial direction catalytic reaction zone (8) and radial with the axis
The internal fluid communication of catalytic reaction zone (8), the other end sealing for unloading agent pipe (10) reach the outside of the shell (2).
9. according to the reactor of claim 3 or 4, wherein the reactor further includes unloading agent pipe for removal catalyst
(10) and for be sucked out catalyst agent device is unloaded, described one end for unloading agent pipe (10) is sealedly attached to axis radial direction catalytic reaction zone
(8) the back cover (18) and the internal fluid communication with axis radial direction catalytic reaction zone (8), unload the other end of agent pipe (10)
Sealing reaches the outsides of the shell (2), described unload agent pipe (10) with catalyst discharge port (9), it is described unload agent device with
The catalyst discharge port (9) is connected.
10. reactor according to claim 1, wherein the lower part of the air inlet pipe (16) is provided at least one for being distributed
It is sent into the gas distributor of the reaction gas of the reactor.
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| 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 |
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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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