CN207102557U - Drawer type reactor - Google Patents
Drawer type reactor Download PDFInfo
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- CN207102557U CN207102557U CN201720810647.XU CN201720810647U CN207102557U CN 207102557 U CN207102557 U CN 207102557U CN 201720810647 U CN201720810647 U CN 201720810647U CN 207102557 U CN207102557 U CN 207102557U
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Abstract
A kind of this disclosure relates to drawer type reactor, the reactor includes horizontal type shell (3), air inlet (1), gas outlet (2), the first end socket (5), the second end socket (4) and the catalyst bed layer frame (9) for placing catalyst, the drawer type reactor also includes the axial slideway (17) being fixed on inside the horizontal type shell, for slidingly supporting the catalyst bed layer frame；First end socket and the second end socket are removably sealingly fastened in the left port and right output port at the housing both ends respectively, and the catalyst bed layer frame slideway level can skid off or slip into the left port or right output port vertically；The air inlet and the gas outlet are located at the top and bottom of the horizontal type shell respectively.The drawer type reactor is easy to handling or more catalyst changeout, simple in construction and simple operation, the structure of reactor that the internal diameter that is particularly suitable for use in is smaller, barrel lenght is longer, solves the problems, such as that operating personnel cannot be introduced into inside reactor and carry out Catalyst packing.
Description
Technical field
This disclosure relates to chemical reactor field, in particular it relates to a kind of drawer type reactor.
Background technology
Fixed bed reactors mainly have a two types, and one kind is vertical fixed-bed reactor, including axially-located bed reaction
Device and radial fixed-bed reactor, another kind of is horizontal type fixed bed reactor.Axially-located bed reactor design, process phase
To easy, simple to operate, but reactor apparatus bulky dimensions, bed pressure drop be present and occur local run aways greatly, easily, move hot delay
Slowly the problems such as, conversion ratio is low, enlarge-effect is obvious.Radial bed reactor ratio of height to diameter is larger, bed pressure drop is small, reactant is being catalyzed
Agent Residence Time is short, but reactant difficult to realize being uniformly distributed diametrically, and designs, complex operation.
In order to overcome the shortcomings of radial bed, while take into account both axially-located bed and radial fixed-bed advantages, it is proposed that Gu
Fixed bed horizontal reactor.Horizontal reactor is in sulphur recovery, methanol-fueled CLC, H2The fields such as S decomposition, denitration have waited until application, take
Obtained preferable Application effect.
Existing horizontal reactor can reduce bed pressure drop in varying degrees, reduce investment, but reaction also be present
Device is complicated, catalyst loading and unloading is difficult and reactor in gas skewness the problems such as.
Utility model content
The purpose of the disclosure is to provide a kind of drawer type reactor, and the space reactor utilization rate is high, bed pressure drop is low, gas
Body is evenly distributed, and catalyst loading and unloading is convenient, simple to operate.
To achieve these goals, the disclosure provides a kind of drawer type reactor, including horizontal type shell, air inlet, outlet
Mouth, the first end socket, the second end socket and the catalyst bed layer frame for placing catalyst；The drawer type reactor also includes being fixed on
Axial slideway inside the horizontal type shell, for slidingly supporting the catalyst bed layer frame；First end socket and
Second end socket is removably sealingly fastened in the left port and right output port at the housing both ends respectively, the catalyst bed layer frame
Slideway level it can skid off or slip into the left port or right output port vertically；The air inlet and the gas outlet are located at respectively
The top and bottom of the housing.
Alternatively, first end socket and the second end socket are sealingly fastened in described by first flange and second flange respectively
In the left port and right output port of housing.
Alternatively, 2~4 beds are arranged at intervals with the housing of the drawer type reactor from top to bottom
Frame, each catalyst bed layer frame lower section are designed with the axial slideway for the Slidable support catalyst bed layer frame.
Alternatively, the catalyst bed layer frame includes top blind flange, bottom support plate and side wall baffle plate, the top blind flange
Expanded metal or woven wire are each independently with bottom support plate.
Alternatively, the catalyst bed layer frame includes the horizontal first end catalytic reaction unit being arranged in order, inside is urged
Change reaction member and the second end catalytic reaction unit, the first end catalytic reaction unit, interior catalyst reaction member and
It is brought into close contact between the adjacent side wall of the second end catalytic reaction unit.
Alternatively, the housing is cylindrical shape or oval cylinder pressure-bearing shell, the left port and right output port to be circular or
Person's ellipse；Or the housing is rectangle tubular pressure-bearing shell, the left port and right output port are rectangle.
Alternatively, the height of the beds is 0.15~0.95 times of the drawer type inside reactor diameter.
Alternatively, the axial slideway includes the first slideway and the second slideway for being set in parallel in same level height, institute
State the first slideway and second slideway is fixedly connected with the inwall of housing respectively.
Alternatively, the drawer type reactor also includes shock resistance gas distribution grid, and the shock resistance gas distribution grid is set
Between the air inlet and the catalyst bed layer frame；The length of the shock resistance gas distribution grid is that drawer type reactor is cut
0.35~0.95 times of line length.
Alternatively, the drawer type reactor also includes gas collection grid, and the gas collection grid is arranged above the gas outlet.
Pass through above-mentioned technical proposal, the drawer type inside reactor of the disclosure are provided with axial slideway, and reactor both sides
End socket is detachable, and the catalyst bed layer frame in reactor can be slided along slideway and take out at end socket or insert reactor, just
In handling or more catalyst changeout, simple in construction and simple operation into reactor.The drawer type reactor is particularly suitable for use in internal diameter
Structure of reactor smaller, barrel lenght is longer, solve operating personnel and cannot be introduced into inside reactor progress Catalyst packing
The problem of.
Other feature and advantage of the disclosure will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing further understanding of the disclosure, and a part for constitution instruction, with following tool
Body embodiment is used to explain the disclosure together, but does not form the limitation to the disclosure.In the accompanying drawings：
Fig. 1 is a kind of structural representation of the embodiment for the drawer type reactor that the disclosure provides；
Fig. 2 is a kind of sectional view (the i.e. A-A faces in Fig. 1 of the embodiment for the drawer type reactor that the disclosure provides
Sectional view)；
Fig. 3 is a kind of vertical view of the catalytic reaction unit of the embodiment for the drawer type reactor that the disclosure provides
Figure；
Fig. 4 is that a kind of catalyst loading and unloading operation order of the embodiment for the drawer type reactor that the disclosure provides is shown
It is intended to；
Fig. 5 is the structural representation of another embodiment for the drawer type reactor that the disclosure provides；
Fig. 6 is sectional view (the i.e. A-A in Fig. 5 of another embodiment for the drawer type reactor that the disclosure provides
The sectional view in face)；
Fig. 7 is the structural representation of the third embodiment of the drawer type reactor that the disclosure provides；
Fig. 8 is sectional view (the i.e. A-A in Fig. 7 of the third embodiment of the drawer type reactor that the disclosure provides
The sectional view in face)；
Fig. 9 is the vertical view of the catalytic reaction unit of the third embodiment of the drawer type reactor that the disclosure provides
Figure；
Figure 10 is that the catalyst loading and unloading operation of the third embodiment of the drawer type reactor that the disclosure provides is suitable
Sequence schematic diagram.
Description of reference numerals
The gas outlet of 1 air inlet 2
The end socket of 3 horizontal type shell 4 second
The shock resistance gas distribution grid of 5 first end socket 6
The second flange of 7 first flange 8
The feed surge area of 9 catalyst bed layer frame 10
The 11 discharging gas collection grids of buffering area 12
The end socket journal stirrup of 13 bottom support plate 14 first
The top blind flange of 15 second end socket journal stirrup 16
Buffering area between the 17 axial beds of slideway 18
The first end catalytic reaction unit of 19 end catalyst reaction member outer baffle 20
The interior catalyst reaction member of 21 the second end catalytic reaction unit 22
The interior catalyst reaction member side wall of 23 first interior catalyst reaction member side wall 24 second
25 end catalyst reaction member Internal baffles
Embodiment
The embodiment of the disclosure 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 explained the disclosure, is not limited to the disclosure.
In the disclosure, in the case where not making opposite explanation, the noun of locality such as " upper and lower, left and right " used typically refers to
Upper and lower, left and right of the device under normal operating condition, specifically may be referred to the page of Figure of description 1." inside and outside " is
Refer to for device profile in itself.
As shown in figure 1, the disclosure provides a kind of drawer type reactor, including horizontal type shell 3, air inlet 1, gas outlet 2,
First end socket 5, the second end socket 4 and the catalyst bed layer frame 9 for placing catalyst；The reactor also includes being fixed on described crouch
Axial slideway 17 inside sandwich type element 3, for slidingly supporting the catalyst bed layer frame 9；First end socket 5 and
Two end sockets 4 are removably sealingly fastened in the left port and right output port at the both ends of horizontal type shell 3 respectively, the catalyst bed
Layer frame 9 level of slideway 17 can skid off or slip into the left port or right output port vertically；The air inlet 1 and the gas outlet
2 are located at the top and bottom of the horizontal type shell 3 respectively.
The drawer type inside reactor of the disclosure is provided with axial slideway, and reactor both sides end socket is detachable, reactor
Interior catalyst bed layer frame can be slided along slideway and take out at end socket or insert reactor, be easy into reactor handling or
More catalyst changeout, simple in construction and simple operation.The drawer type reactor is particularly suitable for use in, and internal diameter is smaller, barrel lenght is longer
Structure of reactor, solve the problems, such as that operating personnel cannot be introduced into inside reactor and carry out Catalyst packing.
According to the disclosure, the mode that the first end socket 5 and the left and right port of the second end socket 4 and horizontal type shell 3 are attached can
Think this area routine, in a kind of embodiment of the disclosure, for the ease of dismounting, the first end socket 5 and the second envelope
First 4 can be sealingly fastened in the left port and right output port of horizontal type shell 3 by first flange 7 and second flange 8 respectively.
According to the disclosure, as shown in Fig. 5-Fig. 6, in order to further improve reaction conversion ratio and reaction efficiency in reactor,
It can be arranged at intervals multiple catalyst bed layer frames 9 in the horizontal type shell 3 of the drawer type reactor from top to bottom, preferably 2~4
Individual, each lower section of catalyst bed layer frame 9 may be provided with the axial slideway 17 for the Slidable support catalyst bed layer frame 9.
According to the disclosure, catalyst bed layer frame 9 is used to place catalyst to form beds, catalyst bed layer frame 9
Concrete form can be that this area is conventional, in order that reacting gas is uniformly distributed in whole beds, avoid out
Existing channel or bias current, the shape of catalyst bed layer frame 9 is preferably according to the determination of the interior shape of reactor, i.e. catalyst bed layer frame 9
Horizontal cross-sectional shape it is identical with the horizontal cross sectional geometry of drawer type reactor.In a kind of embodiment of the disclosure,
Catalyst bed layer frame 9 can include top blind flange 16, bottom support plate 13 and side wall baffle plate, top blind flange 16 and bottom support plate
13 material and concrete form does not limit, as long as disclosure satisfy that bed pressure drop requirement and the machinery needed for loading catalyst
Intensity and do not chemically reacted with material in reaction system, it is preferable that top blind flange 16 and bottom support plate 13 are respective
It independently is expanded metal or woven wire.Inwall of the side wall baffle plate of catalyst bed layer frame 9 preferably with drawer type reactor
It is brought into close contact.
According to the disclosure, for the ease of catalyst loading and unloading, catalyst bed layer frame 9 can include level is arranged in order first
End catalyst reaction member 20, interior catalyst reaction member 22 and the second end catalytic reaction unit 21, above-mentioned catalytic reaction
Unit is used to place catalyst to form beds, and each catalytic reaction unit can be loaded and unloaded individually, easy for installation.Enter one
Step ground, in order to avoid occurring channel, first end catalytic reaction unit 20, interior catalyst reaction member 22 and second in reactor
It can be brought into close contact between the adjacent side wall of end catalyst reaction member 21.Interior catalyst reaction member 22 can be one or
It is brought into close contact the multiple of setting, preferably 2~8.First end catalytic reaction unit 20 and the second end catalytic reaction unit 21
Shape preferably determine that is, the shape of end catalyst reaction member outer baffle 19 preferably the same as connecing therewith according to reactor end socket shape
Tactile end socket shape is identical, as shown in Fig. 2, Fig. 3, Fig. 6.First end catalytic reaction unit 20 and the second end catalytic reaction
The position of unit 21 can be defined by end socket, horizontal type shell 3 and axial slideway 17；The position of interior catalyst reaction member 22
It can be carried out by horizontal type shell 3, first end catalytic reaction unit 20, the second end catalytic reaction unit 21 and axial slideway 17
Limit.Further, for the ease of supporting, under first end catalytic reaction unit 20 and the second end catalytic reaction unit 21
Side can set the first end socket journal stirrup 14 and the second end socket journal stirrup 15 respectively.
According to the disclosure, the shape of horizontal type shell 3 can be that this area is conventional, and housing and end socket material, thickness can be with
Determined according to the reaction process condition of reality.In order to suitable for reaction under high pressure environment, such as when reaction pressure is more than 0.5MPaG,
In a kind of embodiment of the disclosure, as shown in Figure 1-Figure 3, horizontal type shell 3 can be that cylindrical shape or oval cylinder are held
Pressure shell body, left port and right output port can be that shape is corresponding circular or oval.In the another kind specific implementation of the disclosure
In mode, such as when the drawer type reactor is applied into low pressure reaction environment, as reaction pressure be normal pressure to 0.3MPaG when,
As shown in figs. 7 to 9, horizontal type shell 3 can be rectangular cylinder shape pressure-bearing shell, and left port and right output port are correspondingly rectangle.
According to the disclosure, the height of catalyst bed layer frame 9 can be the 0.15~0.95 of drawer type inside reactor diameter
Times, preferably 0.25-0.8 times, most preferably height is 0.5-0.75 times.
According to the disclosure, as shown in Fig. 2 axial slideway 17 can include the first cunning for being set in parallel in same level height
Road and the second slideway, the inwall of the first slideway and the second slideway respectively with horizontal type shell 3 are fixedly connected.Slideway is art technology
Known to personnel, the disclosure does not do any restrictions, as long as the horizontal disengaging housing of catalyst bed layer frame 9 can be realized.Should
When supplementary notes, reacting gas should be avoided to occur channel, short circuit phenomenon at slideway.
According to the disclosure, it is sent into reacting gas for the ease of distribution, prevents reacting gas from directly washing away beds,
In a kind of embodiment of the disclosure, the drawer type reactor also includes a shock resistance gas distribution grid 6, shock resistance gas
Body distribution grid 6 can be arranged at below air inlet 1, in the space reactor of the top of catalyst bed layer frame 9, the shock resistance gas
The length of body distribution grid 6 can be 0.35~0.95 times of reactor tangential length, and preferable length is reactor tangential length
0.55~0.9 times.Further, shock resistance gas distribution grid edge is provided with the acclivitous foldable edge of a circle, folding
Shape side is 30 °~60 °, preferably 45 ° with horizontal plane angle.
According to the disclosure, the gas containing reaction product is sent out for the ease of concentrating, the drawer type reactor can also wrap
Gas collection grid 12 is included, gas collection grid 12 can be arranged at the top of gas outlet 2.
As shown in Fig. 4, Figure 10, the method for catalyst loading and unloading is carried out using the drawer type reactor of the disclosure to be included：
Catalyst bed layer frame 9 or catalytic reaction unit can take out from the left port at end socket or right output port are horizontal, and at end socket
Slideway 17 is horizontally placed in the horizontal type shell 3 vertically for left port or right output port.The method of catalyst change can include：Such as
Shown in Fig. 4, Figure 10, the second end socket 4 connected by second flange 8 is opened, the second end catalysis is extracted out from right output port is sequentially horizontal
Reaction member 21, interior catalyst reaction member 22 and first end catalytic reaction unit 20, fresh catalyst is changed, then sequentially
From right output port horizontally mounted first end catalytic reaction unit 20, the interior catalyst for filling fresh catalyst of slideway 17 vertically
Reaction member 22, the second end catalytic reaction unit 21, finally install the second end socket 4, so as to complete the replacing of a catalyst.
The disclosure is further illustrated by embodiment below in conjunction with accompanying drawing, but therefore the disclosure is not taken office
What is limited.
Embodiment 1
As depicted in figs. 1 and 2, drawer type reactor is provided with air inlet 1 including top used by the present embodiment, bottom is set
There is the cylindrical shape pressure-bearing horizontal type shell 3 of gas outlet 2, the bottom of air inlet 1 is provided with shock resistance gas distribution grid 6, and the top of gas outlet 2 is set
It is equipped with gas collection grid 12.The inwall of horizontal type shell 3 is provided with two axial slideways 17 for being in same level height, in the end socket of both sides
Wall is provided with the first end socket journal stirrup 14 of supporting base end portion catalytic reaction unit, the second end socket journal stirrup 15.End catalyst reaction member
Outer baffle 19, end catalyst reaction member Internal baffle 25, the first interior catalyst reaction member side wall 23, the reaction of the second interior catalyst
Unit sidewall 24 uses the sheet metal that percent opening is 3mm for 5%, hole size, and beds bottom support plate 13 uses
The sheet metal that percent opening is 35%, hole size is 3mm, beds top blind flange 16 use woven wire.
A diameter of 750mm, the tangential length 2500mm of horizontal type shell 3, the length of shock resistance gas distribution grid are
2000mm.Catalyst bed layer frame 9 includes 5 interior catalyst reaction members, 2 end catalyst reaction members are formed, interior catalyst
The axial length 500mm of reaction member, width 440mm, highly it is 550mm, end catalyst reaction member is highly 550mm,
As shown in figure 3, interior catalyst reaction member is not entirely shown.
The reactor of the present embodiment is applied to synthesis gas system and substitutes natural solid/liquid/gas reactions, using cylindrical composite nickel catalyst
Agent, catalyst size areCatalyst volume accounts for the 55% of reactor cumulative volume.Reactor pressure
3.2MPaG, 600 DEG C of temperature, synthesis gas (n (H2)-n(CO2))/ (n(CO)+n(CO2))=3, air speed 10000h-1。
What is provided in table 1 is the drawer type reactor and the contrast situation of axial flow reactor in the prior art of the disclosure.Two kinds
Reactor catalyst loadings, unstripped gas composition and other process conditions are all identical, from the selection of CO conversion ratios, target product
The drawer type reactor that three property, bed pressure drop indexs can be seen that the disclosure all shows more excellent performance, especially
It is that pressure drop aspect advantage is fairly obvious.
The reactor of the embodiment 1 of table 1 contrasts with conventional axial reactor
| Type of reactor | CO conversion ratios/(%) | CH4Selectivity/(%) | Pressure drop/(kPa) |
| Conventional axial reactor | 43 | 95 | 8.2 |
| The reactor of embodiment 1 | 47 | 94 | 2.5 |
Flow using the drawer type reactor more catalyst changeout of the present embodiment is as shown in Figure 4：Opening is connected by second flange 8
The second end socket 4 connect, it is sequentially horizontal to extract the second end catalytic reaction unit 21,5 interior catalyst reaction members 22, first ends out
Portion's catalytic reaction unit 20, replacing fresh catalyst is carried out to catalytic reaction unit.After the completion of replacing, sequentially slideway 17 vertically
Level introduces first end catalytic reaction unit 20,5 interior catalyst reaction members 22, the second ends for filling fresh catalyst
Portion's catalytic reaction unit 21, the second end socket 4 is finally installed, so as to complete the replacing of a methanation reaction catalyst.
Embodiment 2
As shown in Figure 5, Figure 6, the structural parameters such as the present embodiment reactor and the reactor shell internal diameter of embodiment 1, length
It is identical.Difference from Example 1 is there are two catalyst bed layer frames 9 in the present embodiment, is highly 230mm.
The reactor of the present embodiment is applied equally into synthesis gas system and substitutes natural solid/liquid/gas reactions, process conditions and embodiment phase
Together.What is provided in table 2 is the reactor and the contrast situation of axial flow reactor in the prior art of the present embodiment.Two kinds of reactor catalysis
Agent loadings, unstripped gas composition and other process conditions are all identical, from CO conversion ratios, the selectivity of target product, bed pressure drop
The reactor that three indexs can be seen that the present embodiment all shows advantage in terms of more excellent performance, especially pressure drop
It is fairly obvious.
The reactor of the embodiment 2 of table 2 contrasts with axial flow reactor
| Type of reactor | CO conversion ratios/(%) | CH4Selectivity/(%) | Pressure drop/(kPa) |
| Conventional axial reactor | 43 | 95 | 8.2 |
| The reactor of embodiment 1 | 47 | 94 | 2.5 |
| The reactor of embodiment 2 | 47 | 94 | 2.3 |
Embodiment 3
As shown in Figure 7, Figure 8, drawer type reactor shell is rectangle used by the present embodiment, and end socket is metal plate,
Shell dimension is：2500mm*600mm*600mm, the length of shock resistance gas distribution grid is 2000mm, and catalyst bed layer frame 9 is wrapped
5 interior catalyst reaction members are included, end catalyst reaction member is identical with interior catalyst reaction member shape and size, therefore herein
Collectively referred to as interior catalyst reaction member, the axial length 500mm of interior catalyst reaction member, width 600mm, highly it is
400mm, as shown in figure 9, interior catalyst reaction member is not entirely shown.
First interior catalyst reaction member side wall 23, the second interior catalyst reaction member side wall 24 use percent opening for
5%th, hole size is 3mm sheet metal, and it for 35%, hole size is 3mm that beds bottom support plate 13, which uses percent opening,
Sheet metal, beds top blind flange 16 uses woven wire.
The reactor of the present embodiment is washed to periodic off-gases volatile organic matter (VOCs) removing applied to low-temp methanol, adopted
With spherical Pd bases catalyst, catalyst size isCatalyst volume accounts for the 67% of reactor cumulative volume.Reactor pressure
Power 0.03MPaG, 400 DEG C of temperature, CO in periodic off-gases2+N2Volume fraction be 98%, H2O volume fraction is 1%, VOCs's
Volume fraction is about 0.6%, air speed 13000h-1。
Table 3 is the drawer type reactor performance index of the present embodiment.After reactor for treatment, VOCs deviates from periodic off-gases
Rate is 100%, from VOCs removal efficiencies, bed pressure drop two indices can be seen that the disclosure reactor show it is more excellent
Advantage is fairly obvious in terms of different performance, especially pressure drop.
The reactor performance index of the embodiment 3 of table 3
| Type of reactor | VOCs removal efficiencies/(%) | Pressure drop/(kPa) |
| The reactor of embodiment 3 | 100 | 3.5 |
Flow using the drawer type reactor more catalyst changeout of the present embodiment is as shown in Figure 10：Open by second flange 8
Second end socket 4 of connection, it is sequentially horizontal to extract 5 interior catalyst reaction members out, carry out changing fresh catalyst operation, catalysis is anti-
After the completion of the catalyst change for answering unit, 5 inside that sequentially the horizontal introducing of slideway 17 vertically fills fresh catalyst are urged
Change reaction member 22, the second end socket 4 is finally installed, so as to complete the replacing of a VOCs removing Pd base catalyst.
The preferred embodiment of the disclosure is described in detail above in association with accompanying drawing, still, the disclosure is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the disclosure, a variety of letters can be carried out to the technical scheme of the disclosure
Monotropic type, these simple variants belong to the protection domain of the disclosure.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, it can be combined by any suitable means.In order to avoid unnecessary repetition, the disclosure to it is various can
The combination of energy no longer separately illustrates.
In addition, it can also be combined between a variety of embodiments of the disclosure, as long as it is without prejudice to originally
Disclosed thought, it should equally be considered as disclosure disclosure of that.
Claims (10)
1. a kind of drawer type reactor, including horizontal type shell (3), air inlet (1), gas outlet (2), the first end socket (5), the second envelope
Head (4) and the catalyst bed layer frame (9) for placing catalyst；Characterized in that, the drawer type reactor also includes being fixed on
The internal axial slideway (17) of the horizontal type shell (3), for slidingly supporting the catalyst bed layer frame (9)；It is described
First end socket (5) and the second end socket (4) are removably sealingly fastened in left port and the right side at the horizontal type shell (3) both ends respectively
On port, the catalyst bed layer frame (9) slideway (17) level can skid off or slip into the left port or right output port vertically；
The air inlet (1) and the gas outlet (2) are located at the top and bottom of the horizontal type shell (3) respectively.
2. drawer type reactor according to claim 1, it is characterised in that first end socket (5) and the second end socket (4)
It is sealingly fastened in respectively by first flange (7) and second flange (8) in the left port and right output port of the horizontal type shell (3).
3. drawer type reactor according to claim 1, it is characterised in that the horizontal type shell (3) of the drawer type reactor
2~4 catalyst bed layer frames (9) are inside arranged at intervals with from top to bottom, are set below each catalyst bed layer frame (9)
There is the axial slideway (17) for the Slidable support catalyst bed layer frame (9).
4. drawer type reactor according to claim 1, it is characterised in that the catalyst bed layer frame (9) includes top
Cover plate (16), bottom support plate (13) and side wall baffle plate, the top blind flange (16) and bottom support plate (13) are independently of one another
For expanded metal or woven wire.
5. drawer type reactor according to claim 1, it is characterised in that the catalyst bed layer frame (9) includes level
First end catalytic reaction unit (20), interior catalyst reaction member (22) and the second end catalytic reaction unit being arranged in order
(21), the first end catalytic reaction unit (20), interior catalyst reaction member (22) and the second end catalytic reaction unit
(21) it is brought into close contact between adjacent side wall.
6. drawer type reactor according to claim 1, it is characterised in that the horizontal type shell (3) is cylindrical shape or ellipse
Cylindrical shape pressure-bearing shell, the left port and right output port are circular or ellipse；Or the horizontal type shell (3) is rectangular cylinder
Shape pressure-bearing shell, the left port and right output port are rectangle.
7. drawer type reactor according to claim 1, it is characterised in that the height of the catalyst bed layer frame (9) is
0.15~0.95 times of the drawer type inside reactor diameter.
8. drawer type reactor according to claim 1, it is characterised in that the axial slideway (17) includes be arrangeding in parallel
In the first slideway and the second slideway of same level height, first slideway and second slideway respectively with horizontal type shell
(3) inwall is fixedly connected.
9. drawer type reactor according to claim 1, it is characterised in that the drawer type reactor also includes shock resistance gas
Body distribution grid (6), the shock resistance gas distribution grid (6) be arranged at the air inlet (1) and the catalyst bed layer frame (9) it
Between；The length of the shock resistance gas distribution grid (6) is 0.35~0.95 times of drawer type reactor tangential length.
10. drawer type reactor according to claim 1, it is characterised in that the drawer type reactor also includes gas collection lattice
Grid (12), the gas collection grid (12) are arranged above the gas outlet (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720810647.XU CN207102557U (en) | 2017-07-05 | 2017-07-05 | Drawer type reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720810647.XU CN207102557U (en) | 2017-07-05 | 2017-07-05 | Drawer type reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207102557U true CN207102557U (en) | 2018-03-16 |
Family
ID=61587672
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720810647.XU Active CN207102557U (en) | 2017-07-05 | 2017-07-05 | Drawer type reactor |
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| CN (1) | CN207102557U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108534111A (en) * | 2018-04-03 | 2018-09-14 | 李根钧 | A kind of energy conservation and environmental protection system applied in combustion apparatus |
| CN115138298A (en) * | 2022-09-05 | 2022-10-04 | 山东新港化工有限公司 | Production device for dehydrogenation reaction of o-phenylphenol and use method thereof |
-
2017
- 2017-07-05 CN CN201720810647.XU patent/CN207102557U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108534111A (en) * | 2018-04-03 | 2018-09-14 | 李根钧 | A kind of energy conservation and environmental protection system applied in combustion apparatus |
| CN108534111B (en) * | 2018-04-03 | 2020-01-17 | 李根钧 | Energy-saving and environment-friendly system applied to combustion equipment |
| CN115138298A (en) * | 2022-09-05 | 2022-10-04 | 山东新港化工有限公司 | Production device for dehydrogenation reaction of o-phenylphenol and use method thereof |
| CN115138298B (en) * | 2022-09-05 | 2022-11-18 | 山东新港化工有限公司 | Production device for o-phenylphenol dehydrogenation reaction and use method thereof |
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