CN208959856U - A kind of axial-radial flow reactor - Google Patents
A kind of axial-radial flow reactor Download PDFInfo
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- CN208959856U CN208959856U CN201821550291.1U CN201821550291U CN208959856U CN 208959856 U CN208959856 U CN 208959856U CN 201821550291 U CN201821550291 U CN 201821550291U CN 208959856 U CN208959856 U CN 208959856U
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Abstract
The utility model relates to the technical fields of coal chemical industry synthesizer, and in particular to a kind of axial-radial flow reactor.Including upper cover, cylinder, reaction mechanism, lower head and skirt；The top of the upper cover offers air inlet, and the two sides of air inlet are symmetrically arranged with water inlet, and the two sides of upper cover adjacent with water inlet are equipped with water outlet；Whirlwind distributor is equipped in the upper cover, the whirlwind distributor is connected to air inlet；Water collection tank, upper porcelain layers of balls, catalyst bed and support porcelain layers of balls are from top to bottom successively arranged in the cylinder；The water collection tank, upper porcelain layers of balls, catalyst bed and support porcelain layers of balls constitute reaction mechanism；Porcelain ball is loaded in upper porcelain layers of balls, support porcelain layers of balls and lower head respectively, the porcelain spherolite diameter loaded in lower head is greater than the porcelain spherolite diameter loaded in support porcelain layers of balls；It can solve that traditional reactor loaded catalyst is small, and pressure drop is big, the high problem of reaction tube material grade.
Description
Technical field
The utility model relates to the technical fields of coal chemical industry synthesizer, and in particular to a kind of axial-radial flow reactor.
Background technique
Currently, the reactor apparatus in coal chemical technology synthesizer, including methyl alcohol synthetic reactor, ethylene glycol synthetic tower etc.,
Axial restraint tube-sheet type consersion unit is generally used, synthesis gas enters in reactor from tube side import, the catalyst in reaction tube
Effect is lower to carry out synthetic reaction, and reaction heat is taken away by shell side water.It is illustrated in figure 7 traditional axial restraint tube-sheet type reaction
Device, tube side medium are reaction gas, and shell side medium is water.Catalyst packing utilizes the water of shell side, absorbing reaction in heat exchanger tube
Heat realizes the purpose for utilizing steam generation by reaction heat to play stable reaction temperature.Above-mentioned traditional structure of reactor, is deposited
In following defect: (1) since the temperature of pipe, shell side is variant, the heat between tube side (heat exchanger tube) and shell side (shell-side cylinder) is swollen
Bulk is inconsistent, and thermal expansion amount is poor in order to control, and leads to the generally not super 7000mm of the heat exchanger tube length of the reactor, and exchange heat pipe range
Degree limits the loadings of catalyst, and then limits the production capacity of separate unit reactor；(2) due to the characteristic of pipe, shell side medium, with
And catalyst, to material requirement, shell side selects carbon steel material under normal circumstances, and tube side (heat exchanger tube) needs to select stainless steel
The material of the above rank.Even if controlling the length of heat exchanger tube, due to line expansion system between common austenitic stainless steel and carbon steel
Number difference is larger, and thermal expansion still cannot be met the requirements, and heat exchanger tube needs to select the higher two phase stainless steel of material rate, causes
The cost of reactor increases considerably because using special two phase stainless steel；(3) since Catalyst packing is in heat exchanger tube
Portion, heat exchanger tube diameter is typically small, is mostly 44mm or 38mm.Whole reactor loadings simultaneously by heat exchanger tube diameter and
The limitation of heat exchanger tube length constrains the loadings of catalyst, and then limits the production capacity of separate unit reactor；(4) due to structure
The reason of, traditional reactor synthesis gas extends axially through catalyst bed, and thickness of bed layer is thicker, and technique side pressure drop is larger, causes
Energy loss is larger.
Utility model content
The shortcomings that the utility model aim is to improve prior art provides a kind of axial-radial flow reactor, can solve biography
Reactor catalyst loadings of uniting are small, and pressure drop is big, the high problem of reaction tube material grade.
A kind of axial-radial flow reactor, the axial-radial flow reactor from top to bottom successively include upper cover 3, cylinder 11, reaction
Mechanism, lower head 20 and skirt 22；The top of the upper cover 3 offers air inlet 1, the two sides of air inlet 1 be symmetrically arranged with into
The two sides at the mouth of a river 2, upper cover 3 adjacent with water inlet 2 are equipped with water outlet 4；Whirlwind distributor 5 is equipped in the upper cover 3, it is described
The inlet end of whirlwind distributor 5 is connected to air inlet 1；Water collection tank, upper porcelain ball are from top to bottom successively arranged in the cylinder 11
Layer 10, catalyst bed 12 and support porcelain layers of balls 18；The water collection tank, upper porcelain layers of balls 10, catalyst bed 12 and support porcelain
Layers of balls 18 constitutes reaction mechanism；Upper porcelain layers of balls 10 supports and loads porcelain ball in porcelain layers of balls 18 and lower head 20 respectively, in lower head 20
The porcelain spherolite diameter of filling is greater than the porcelain spherolite diameter loaded in support porcelain layers of balls 18；
The water collection tank includes the effluent collection case 8 of the water inlet collecting box 6 and lower part on top, the water inlet collecting box 6
Bottom plate be upper perforated plate 7, the bottom plate of the effluent collection case 8 is lower perforated plate 9, and water inlet collecting box 6 is connected to by pipeline into water
Mouth 2, effluent collection case 8 is connected to water outlet 4 by pipeline；First is axially formed between the water inlet collecting box 6 and upper cover 3
Air-inlet cavity is axially formed the second air-inlet cavity between the effluent collection case 8 and upper porcelain layers of balls 10；It is coaxially provided in the cylinder 11
The central tube 14 of upper end closed, the central tube 14 are from top to bottom sequentially passed through in upper porcelain layers of balls 10, catalyst bed 12, support
Porcelain layers of balls 18 and lower head 20, and the gas outlet 24 opened up with 20 bottom end of lower head is connected to；Corresponding in catalyst bed 12
Central tube is laid on 14 side wall of heart pipe；
The catalyst bed 12 includes several heat exchanger tubes and side wall distributor 13 that are axially arranged, the heat exchanger tube by
The outer tube 17 and inner tube 16 of coaxial arrangement form, and 16 bottom end of inner tube and 17 bottom end of outer tube of every heat exchanger tube are equipped with spacing, described
The surrounding that several heat exchanger tube central symmetries are distributed in central tube 14 forms cylindric nest of tubes；Along the pipe shaft etc. of several heat exchanger tubes
Spacing is equipped with the second support plate 171 of 2 pieces of level above, and the lower end of the outer tube 17 extends in support porcelain layers of balls 18, described
The upper end of outer tube 17 extends in effluent collection case 8, and the upper end tube nozzle of outer tube 17 is installed on lower perforated plate 9, and adjacent outer tube
Loading catalyst in gap between 17；The upper end of said inner tube 16 is extended into water collecting box 6, and the upper pipes of inner tube 16
Mouth is installed on upper perforated plate 7；
The side wall distributor 13 is cannula-like, and coaxial sleeve is set on the nest of tubes that several heat exchanger tubes are formed, the side wall
The upper end of distributor 13 is fixed on 11 inner wall of cylinder by connecting plate 131, and lower end is fixed on 11 inner wall of cylinder by ring flat-plate 132
On, and third air-inlet cavity is axially formed between 11 inner wall of the side wall distributor 13 and cylinder, on the side wall distributor 13
It is laid with areole；When work, synthesis gas enters in reactor from air inlet 1, forms primary uniform point through whirlwind distributor 5
Cloth, after through the first air-inlet cavity, the second air-inlet cavity, third air-inlet cavity and side wall distributor 13 formed secondary uniform distribution so that
The synthesis gas and catalyst that radial direction penetrates in catalyst bed 12 come into full contact with reaction, and the gas after reaction enters in central tube 14
Reactor is discharged from gas outlet 24；Simultaneously water enter from water inlet 2 into water collecting box 6, subsequently into inner tube 16, then from
Away from the annular space space entered between inner tube 16 and outer tube 17, most it is discharged afterwards through effluent collection case 8 from water outlet 4, water passes through inner tube
Absorbing reaction heat when annular space space between 16 and outer tube 17, thus byproduct steam.
Further, the gross area of the central tube and the gross area of areole are equal, and are 13 He of side wall distributor
2 ~ 2.5 times of the annulus area that 11 inner wall of cylinder is formed；The aperture of the central tube and areole is catalyst particle size
0.5 ~ 0.8 times.
Further, the first inlet chamber height be 2500 ~ 3000mm, the second inlet chamber height be 1500 ~
2000mm；The third inlet chamber height is 200mm or more, and meets the annulus that side wall distributor 13 and 11 inner wall of cylinder are formed
Area is 2 times of 1 cross-sectional area of air inlet.
Further, 16 diameter of said inner tube is 16 ~ 44mm, and 17 diameter of outer tube is 32 ~ 57mm, the central tube 14
Diameter is 800 ~ 1500mm.
Further, the height of the upper porcelain layers of balls 10 is 100 ~ 200mm.
Further, 18 height of support porcelain layers of balls is 200 ~ 300mm.
Further, the lower end of the central tube 14 is equipped with central tube pedestal 23 with suitable.
Further, the lower end of the outer tube 17 extends in support porcelain layers of balls 18, and extending depth is 100mm.
Further, the bottom radial symmetric of the lower head 20 is equipped with catalyst discharge port 21.
Further, 2 groups or more gusseteds, every group of triangle branch are equidistantly equipped on the outer wall of said inner tube 16 along pipe shaft
Support includes three the first support plates 161 radially arranged along inner tube 16.
The advantageous effects of the utility model include:
1, the novel axial-radial flow reactor reactor of the utility model, heat exchanger tube are optimized for one by both ends fixed tube sheet type
End fix, the other end can free expansion type inner tube set be set to outer tube in heat exchanger tube；Catalyst is by being seated in tube side (heat exchange
In pipe) it is optimized for being seated in shell side (outside heat exchanger tube), realize that tube side is leaked water, loading catalyst in shell side；The catalysis of cross section
Agent loadings can increase by 30% or more compared with traditional approach, and realize heat exchanger tube can free wxpansion, solve heat exchanger tube and shell side
The problem of swell increment difference between cylinder, so that solving heat exchanger tube needs asking using the higher two phase stainless steel of material rate
Topic, heat exchanger tube only need to can reduce 30% or more equipment manufacturing cost using common stainless steel；While the length of heat exchanger tube is no longer
It is the restraining factors for influencing loaded catalyst, heat exchanger tube length can increase to 12500mm from 7000mm；From heat exchanger tube length
Consider, compare traditional reactor, catalysis loadings can be improved 50% or more, can increase substantially the production capacity of separate unit reactor.
2, the utility model change traditional reactor synthesis gas extends axially through catalyst bed, and thickness of bed layer is thicker, work
Skill side pressure drop is larger, causes energy loss big, the utility model reaction gas is directed radially through catalyst bed, greatly reduces conjunction
At gas by the thickness of reaction bed, 50% or more technique side pressure drop can be reduced.
3, synthesis gas is once evenly distributed to synthesis gas the inside of reactor by whirlwind distributor, whirlwind distributor,
After through the first air-inlet cavity, the second air-inlet cavity, third air-inlet cavity and side wall distributor form secondary uniform distribution worn so that radial
The synthesis gas and catalyst entered in catalyst bed comes into full contact with, reaction more sufficiently, increase reaction efficiency, while inner tube and outer
The reaction heat of synthetic reaction generation is taken away in boiler feedwater in pipe ring gap, to play stable reaction temperature, realizes and utilizes reaction
The purpose of hot byproduct steam.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the novel axial-radial flow reactor of the utility model.
Fig. 2 is the A-A cross-sectional view of novel axial-radial flow reactor.
Fig. 3 is the B-B cross-sectional view of novel axial-radial flow reactor.
Fig. 4 is the partial structural diagram of single heat exchange tube.
Fig. 5 is the partial enlarged view of structure I.
Fig. 6 is the structural schematic diagram of inner tube support.
Fig. 7 is axial restraint tube-sheet type reactor.
Wherein: 1- air inlet；11- cylinder；2- water inlet；3- upper cover；4- water outlet；5- whirlwind distributor；6- water inlet
Collecting box；7- upper perforated plate；8- effluent collection case；9- lower perforated plate；The upper porcelain layers of balls of 10-；11- cylinder；12- catalyst bed；The side 13-
Wall distributor；131- connecting plate；132- ring flat-plate；14- central tube, 16- inner tube；The first support plate of 161-；17 outer tubes；171- second
Support plate；18- supports porcelain layers of balls；20- lower head；21- catalyst discharge port；22- skirt；23- central tube pedestal；24- outlet
Mouthful.
Specific embodiment
In order to make the purpose of the utility model, technical solutions and advantages more clearly understood, below in conjunction with attached drawing 1 ~ 6 and in fact
Example is applied, the present invention will be further described in detail.It should be appreciated that the specific embodiments described herein are only used to
It explains the utility model, is not used to limit the utility model.
A kind of axial-radial flow reactor, reactor diameter 4000mm, the axial-radial flow reactor from top to bottom successively include
Upper cover 3, cylinder 11, lower head 20 and skirt 22；The top of the upper cover 3 offers air inlet 1, the two sides of air inlet 1
It is symmetrically arranged with water inlet 2, the two sides of upper cover 3 adjacent with water inlet 2 are equipped with water outlet 4；Equipped with whirlwind point in the upper cover 3
Cloth device 5,5 air intake of whirlwind distributor are connected to air inlet 1；Water collection is from top to bottom successively arranged in the cylinder 11
Case, upper porcelain layers of balls 10, catalyst bed 12 and support porcelain layers of balls 18；The water collection tank, upper porcelain layers of balls 10, catalyst bed 12
Reaction mechanism is constituted with support porcelain layers of balls 18；Porcelain ball is loaded respectively in upper porcelain layers of balls 10, support porcelain layers of balls 18 and lower head 20, under
The porcelain spherolite diameter loaded in end socket 20 is greater than the porcelain spherolite diameter loaded in support porcelain layers of balls 18；
The water collection tank includes the effluent collection case 8 of the water inlet collecting box 6 and lower part on top, the water inlet collecting box 6
Bottom plate be upper perforated plate 7, the bottom plate of the effluent collection case 8 is lower perforated plate 9, and water inlet collecting box 6 is connected to by pipeline into water
Mouth 2, effluent collection case 8 is connected to water outlet 4 by pipeline；First is axially formed between the water inlet collecting box 6 and upper cover 3
Air-inlet cavity, and height is 2500mm, the second air-inlet cavity is axially formed between the effluent collection case 8 and upper porcelain layers of balls 10, and high
Degree is 1800mm；The central tube 14 of upper end closed is coaxially provided in the cylinder 11, the central tube 14 from top to bottom successively passes through
It is through at porcelain layers of balls 10, catalyst bed 12, support porcelain layers of balls 18 and lower head 20, and the outlet opened up with 20 bottom end of lower head
Mouth 24 is connected to；Corresponding to being laid with central tube on 14 side wall of central tube of catalyst bed 12；The catalyst bed 12
Including several heat exchanger tubes being axially arranged and side wall distributor 13, described heat exchanger tube includes the inner tube 16 of coaxial arrangement and outer
Pipe 17, the surrounding that several heat exchanger tube central symmetries are distributed in central tube 14 form cylindric nest of tubes；
The heat exchanger tube is made of the outer tube 17 and inner tube 16 being coaxially disposed, and the pipe shaft along the outer tube 17 is equidistantly equipped with
4 pieces of second horizontal support plates 171, the lower end of the outer tube 17 extend in support porcelain layers of balls 18, the upper end of the outer tube 17
It extends in effluent collection case 8, and the upper end tube nozzle of outer tube 17 is installed on lower perforated plate 9, in the gap between adjacent outer tube 17
Loading catalyst；16 bottom end of said inner tube and 17 bottom end of outer tube are equipped with spacing, and the upper end of said inner tube 16 is extended to collects into water
In case 6, and the upper end tube nozzle of inner tube 16 is installed on upper perforated plate 7；Heat exchanger tube length is 12500mm, due to inner tube 16 and outer tube
17 material is identical, and thermal expansion amount is consistent, so that heat exchanger tube length increases, is no more than by the heat exchanger tube length of original reactor
7000mm increases to 12500mm, increases heat exchange amount, increases the production capacity of separate unit axis radial direction heat exchanger；
The side wall distributor 13 is cannula-like, and coaxial sleeve is set on the nest of tubes that several heat exchanger tubes are formed, and the side
Wall distributor 13 is located at the outside of catalyst bed 12, and the upper end of the side wall distributor 13 is installed in cylinder by connecting plate 131
On 11 inner wall of body, lower end is fixed on 11 inner wall of cylinder by ring flat-plate 132, and the side wall distributor 13 and 11 inner wall of cylinder it
Between be axially formed third air-inlet cavity, be highly 300mm, be laid with areole on the side wall distributor 13；The central tube
Hole and the aperture of areole are 0.5 ~ 0.8 times of catalyst particle size；
When work, synthesis gas enters in reactor from air inlet 1, is formed through whirlwind distributor 5 and is once uniformly distributed, later
Secondary uniform distribution is formed through the first air-inlet cavity, the second air-inlet cavity, third air-inlet cavity and side wall distributor 13, so that radial penetrate
Synthesis gas and catalyst in catalyst bed 12 come into full contact with reaction, and the gas after reaction enters in central tube 14 from gas outlet
24 discharge reactors；Water is entered from water inlet 2 into water collecting box 6 simultaneously, subsequently into inner tube 16, then out of spacing entrance
Annular space space between pipe 16 and outer tube 17 is most discharged through effluent collection case 8 from water outlet 4 afterwards, and water passes through inner tube 16 and outer tube
Absorbing reaction heat when annular space space between 17, thus byproduct steam.
Further, the area equation of the area of the central tube and areole, and be side wall distributor 13 and cylinder
2 ~ 2.5 times of the annulus area that 11 inner walls are formed.Guarantee that synthetic gas can pass through side wall distributor 13, into catalytic machine
Bed 12, byproduct steam enters gas outlet 24 from central tube 14 reactor is discharged after reaction, and it is extra or not will cause synthesis gas
The situation of foot.
Further, the annulus area that side wall distributor 13 and 11 inner wall of cylinder are formed is the 2 of 1 cross-sectional area of air inlet
Times.So that reaction is sufficiently efficient.
Further, 16 diameter of said inner tube is 32mm, and 17 diameter of outer tube is 44mm, and 14 diameter of central tube is
1200mm。
Further, the height of the upper porcelain layers of balls 10 is 150mm.
Further, 18 height of support porcelain layers of balls is 300mm.
Further, the lower end of the central tube 14 is equipped with central tube pedestal 23 with suitable.The placement of support central tube 14
Stablize.
Further, the lower end of the outer tube 17 extends in support porcelain layers of balls 18, and extending depth is 100mm.
Further, the bottom radial symmetric of the lower head 20 is equipped with catalyst discharge port 21.It is convenient for changing lower head
The catalyst filled in 20.
Further, 2 groups of gusseteds, every group of gusseted packet are equidistantly equipped on the outer wall of said inner tube 16 along pipe shaft
Include three the first support plates 161 radially arranged along inner tube 16.Prevent inner tube 16 from trembling when in use, influence using.
As it will be easily appreciated by one skilled in the art that the above is only the preferred embodiment of the utility model only, not
To limit the utility model, any modification made within the spirit and principle of the present invention, equivalent replacement and change
Into etc., it should be included within the scope of protection of this utility model.
Claims (10)
1. a kind of axial-radial flow reactor, it is characterised in that: the axial-radial flow reactor from top to bottom successively include upper cover (3),
Cylinder (11), reaction mechanism, lower head (20) and skirt (22)；
The top of the upper cover (3) offers air inlet (1), and the two sides of air inlet (1) are symmetrically arranged with water inlet (2), with into
The two sides of the adjacent upper cover (3) in the mouth of a river (2) are equipped with water outlet (4)；Whirlwind distributor (5) are equipped in the upper cover (3), it is described
The inlet end of whirlwind distributor (5) is connected to air inlet (1)；
Water collection tank, upper porcelain layers of balls (10), catalyst bed (12) and support are from top to bottom successively arranged in the cylinder (11)
Porcelain layers of balls (18)；The water collection tank, upper porcelain layers of balls (10), catalyst bed (12) and support porcelain layers of balls (18) constitute reaction machine
Structure；Porcelain ball, the porcelain loaded in lower head (20) are loaded in upper porcelain layers of balls (10), support porcelain layers of balls (18) and lower head (20) respectively
Spherolite diameter is greater than the porcelain spherolite diameter loaded in support porcelain layers of balls (18)；
The water collection tank includes the water inlet collecting box (6) on top and the effluent collection case (8) of lower part, the water inlet collecting box
(6) bottom plate is upper perforated plate (7), and the bottom plate of the effluent collection case (8) is lower perforated plate (9), and water inlet collecting box (6) passes through pipeline
It is connected to water inlet (2), effluent collection case (8) is connected to water outlet (4) by pipeline；The water inlet collecting box (6) and upper envelope
Head (3) between be axially formed the first air-inlet cavity, be axially formed between the effluent collection case (8) and upper porcelain layers of balls (10) second into
Wind chamber；The central tube (14) of upper end closed is coaxially provided in the cylinder (11), the central tube (14) is from top to bottom successively passed through
Be through at porcelain layers of balls (10), catalyst bed (12), support porcelain layers of balls (18) and lower head (20), and with lower head (20) bottom end
Gas outlet (24) connection opened up；Corresponding to being laid with central tube on central tube (14) side wall of catalyst bed (12)；
The catalyst bed (12) includes several heat exchanger tubes and side wall distributor (13) being axially arranged；The heat exchanger tube by
The outer tube (17) and inner tube (16) of coaxial arrangement form, between inner tube (16) bottom end and outer tube (17) bottom end of every heat exchanger tube are equipped with
Away from；
The surrounding that several heat exchanger tube central symmetries are distributed in central tube (14) forms columned nest of tubes, along described several
The pipe shaft of root heat exchanger tube is equidistantly equipped with second support plate (171) of 2 pieces of level above；The outer tube of several heat exchanger tubes
(17) lower end extends in support porcelain layers of balls (18), and the upper end of the outer tube (17) extends in effluent collection case (8), and outer tube
(17) upper end tube nozzle is installed on lower perforated plate (9), loading catalyst in the gap between adjacent outer tube (17)；Described several
The upper end of the inner tube (16) of heat exchanger tube is extended into water collecting box (6), and the upper end tube nozzle of inner tube (16) is installed in upper perforated plate
(7) on；
The side wall distributor (13) is cannula-like, and coaxial sleeve is set on the nest of tubes that several heat exchanger tubes are formed, the side wall point
The upper end of cloth device (13) is fixed on cylinder (11) inner wall by connecting plate (131), and lower end is installed in cylinder by ring flat-plate (132)
(11) on inner wall, areole is laid on the side wall distributor (13)；The external cylindrical surface of the side wall distributor (13) with
Circular third air-inlet cavity is axially formed between cylinder (11) inner wall；
When work, synthesis gas enters in reactor from air inlet (1), is formed through whirlwind distributor (5) and is once uniformly distributed, later
Secondary uniform distribution is formed through the first air-inlet cavity, the second air-inlet cavity, third air-inlet cavity and side wall distributor (13), so that radial wear
The synthesis gas and catalyst entered in catalyst bed (12) comes into full contact with reaction, the gas after reaction enter in central tube (14) from
Reactor is discharged in gas outlet (24)；Water is entered from water inlet (2) into water collecting box (6) simultaneously, subsequently into inner tube (16),
Enter the annular space space between inner tube (16) and outer tube (17) from the spacing of inner tube (16) and outer tube (17) lower end again, most afterwards through going out
Water collection tank (8) is discharged from water outlet (4), absorbing reaction when water passes through the annular space space between inner tube (16) and outer tube (17)
Heat, thus byproduct steam.
2. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the gross area and side wall of the central tube
The gross area in hole is equal, and 2 ~ 2.5 times of the annulus area formed for side wall distributor (13) and cylinder (11) inner wall；In described
The aperture of heart pore and the aperture of areole are 0.5~0.8 times of catalyst particle size.
3. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the first air-inlet cavity height be 2500 ~
3000mm；The second air-inlet cavity height is 1500 ~ 2000mm；The third air-inlet cavity height is 200mm or more, side wall distribution
The annulus area that device (13) and cylinder (11) inner wall are formed is 2 times of air inlet (1) cross-sectional area.
4. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: said inner tube (16) diameter is 16 ~ 44mm,
Outer tube (17) diameter is 32 ~ 57mm, and central tube (14) diameter is 800 ~ 1500mm.
5. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the height of the upper porcelain layers of balls (10) is
100~200mm。
6. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the support porcelain layers of balls (18) is highly
200~300mm。
7. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the lower end of the central tube (14) is set with suitable
There are central tube pedestal (23).
8. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the lower end of the outer tube (17) extends to branch
It supports in porcelain layers of balls (18), and extending depth is 100mm.
9. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: the bottom of the lower head (20) is radially right
Claim to be equipped with catalyst discharge port (21).
10. a kind of axial-radial flow reactor according to claim 1, it is characterised in that: along pipe on the outer wall of said inner tube (16)
Body is equidistantly equipped with 2 groups or more gusseteds, and every group of gusseted includes three the first supports radially arranged along inner tube (16)
Plate (161).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821550291.1U CN208959856U (en) | 2018-09-21 | 2018-09-21 | A kind of axial-radial flow reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821550291.1U CN208959856U (en) | 2018-09-21 | 2018-09-21 | A kind of axial-radial flow reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208959856U true CN208959856U (en) | 2019-06-11 |
Family
ID=66757550
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821550291.1U Withdrawn - After Issue CN208959856U (en) | 2018-09-21 | 2018-09-21 | A kind of axial-radial flow reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208959856U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108905906A (en) * | 2018-09-21 | 2018-11-30 | 东华工程科技股份有限公司 | A kind of axial-radial flow reactor |
-
2018
- 2018-09-21 CN CN201821550291.1U patent/CN208959856U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108905906A (en) * | 2018-09-21 | 2018-11-30 | 东华工程科技股份有限公司 | A kind of axial-radial flow reactor |
| CN108905906B (en) * | 2018-09-21 | 2023-09-19 | 东华工程科技股份有限公司 | Axial-radial reactor |
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