CN207102556U - Horizontal reactor - Google Patents
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- CN207102556U CN207102556U CN201720810634.2U CN201720810634U CN207102556U CN 207102556 U CN207102556 U CN 207102556U CN 201720810634 U CN201720810634 U CN 201720810634U CN 207102556 U CN207102556 U CN 207102556U
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Abstract
A kind of this disclosure relates to horizontal reactor, the horizontal reactor is internally provided with axial slideway, and reactor both sides end socket is detachable, catalyst bed layer frame in reactor can be slided along slideway and take out or insert reactor at end socket, it is easy to handling or more catalyst changeout, simple in construction and simple operation into reactor.The horizontal reactor is particularly suitable for use in the structure of reactor that internal diameter 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.In addition, heat-exchanging component is provided with the horizontal reactor, fresh feed gas enters the preheating material air inlet positioned at reactor head after heat-exchanging component raises temperature, improve the material temperature into reactor, reduce reacting product outlet temperature, energy utilization efficiency is not only increased, the function also with regulation reactor self heat balance.
Description
Technical field
This disclosure relates to chemical reactor field, in particular it relates to a kind of horizontal 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 horizontal reactor, and the space reactor utilization rate is high, bed pressure drop is low, gas
It is evenly distributed, catalyst loading and unloading is convenient, simple to operate.
To achieve these goals, the disclosure provides a kind of horizontal reactor, and the horizontal reactor includes housing, air inlet
Mouth, gas outlet, the first end socket, the second end socket, preheating material air inlet, preheating material outlet, heat-exchanging component, axial slideway and urge
Agent bed frame；The axial slideway is fixed on the enclosure interior, 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, institute
State catalyst bed layer frame slideway level can skid off or slip into the left port or right output port vertically；The air inlet, preheating
Material outlet and the gas outlet are located at the bottom of the housing, and the preheating material air inlet is located at the top of the housing；
The air inlet is exported with the preheating material and connected by being arranged at the heat-exchanging component of the enclosure interior, the preheating material
Outlet is connected with the air inlet by being arranged at the connecting pipeline of the hull outside.
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, 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, the height of the catalyst bed layer frame is described horizontal
0.15~0.95 times of inside reactor diameter.
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 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, 2~4 catalyst bed layer frames are arranged at intervals with the housing of the horizontal reactor from top to bottom,
The axial slideway for the Slidable support catalyst bed layer frame is designed with below each catalyst bed layer frame.
Alternatively, the heat-exchanging component is below all catalyst bed layer frames.
Alternatively, the horizontal reactor also includes gas distributor, and the gas distributor is arranged at the preheating material
Below air inlet.
Alternatively, the horizontal reactor also includes gas collection grid, and the gas collection grid is arranged at the heat-exchanging component and institute
State between gas outlet.
Pass through above-mentioned technical proposal, the horizontal reactor of the disclosure are internally provided with axial slideway, and the side seal of reactor two
Head is detachable, and the catalyst bed layer frame in reactor can be slided along slideway and take out at end socket or insert reactor, be easy to
Handling or more catalyst changeout, simple in construction and simple operation into reactor.The horizontal reactor be particularly suitable for use in internal diameter it is smaller,
The longer structure of reactor of barrel lenght, solve operating personnel and cannot be introduced into asking for inside reactor progress Catalyst packing
Topic.In addition, being provided with heat-exchanging component in the horizontal reactor, fresh feed gas enters back into position after heat-exchanging component raises temperature
In the preheating material air inlet of reactor head, improve the material temperature into reactor, reduce reacting product outlet temperature
Degree, energy utilization efficiency is not only increased, the function also with regulation reactor self heat balance.
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 horizontal 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 horizontal reactor that the disclosure provides
Sectional view)；
Fig. 3 is a kind of top view of the catalytic reaction unit of the embodiment for the horizontal reactor that the disclosure provides；
Fig. 4 is a kind of catalyst loading and unloading operation order signal of the embodiment for the horizontal reactor that the disclosure provides
Figure；
Fig. 5 is the structural representation of another embodiment for the horizontal reactor that the disclosure provides；
Fig. 6 is sectional view (the i.e. A-A faces in Fig. 5 of another embodiment for the horizontal reactor that the disclosure provides
Sectional view)；
Fig. 7 is the structural representation of the third embodiment of the horizontal reactor that the disclosure provides；
Fig. 8 is sectional view (the i.e. A-A faces in Fig. 7 of the third embodiment of the horizontal reactor that the disclosure provides
Sectional view)；
Fig. 9 is the vertical view of the catalytic reaction unit of the third embodiment of the horizontal reactor that the disclosure provides
Figure；
Figure 10 is the catalyst loading and unloading operation order of the third embodiment of the horizontal reactor that the disclosure provides
Schematic diagram.
Description of reference numerals
The gas outlet of 1 preheating material air inlet 2
The end socket of 3 housing 4 second
The gas distributor 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
The preheating material of 25 end catalyst reaction member Internal baffle 26 exports
The air inlet of 27 heat-exchanging component 28
29 connecting pipelines.
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 horizontal reactor, the horizontal reactor includes housing 3, air inlet 28, gone out
Gas port 2, the first end socket 5, the second end socket 4, preheating material air inlet 1, preheating material outlet 26, heat-exchanging component 27, axial slideway
17 and catalyst bed layer frame 9；The axial slideway 17 is fixed on inside the housing 3, for slidingly supporting described urge
Agent bed frame 9；The end socket 4 of first end socket 5 and second is removably sealingly fastened in the left end at the both ends of housing 3 respectively
On mouth and right output port, the catalyst bed layer frame 9 level of slideway 17 can skid off or slip into the left port or right-hand member vertically
Mouthful；The air inlet 28, preheating material outlet 26 and the gas outlet 2 are located at the bottom of the housing 3, and the preheating material enters
Gas port 1 is located at the top of the housing 3；The air inlet 28 and preheating material outlet 26 are by being arranged at the housing 3
Internal heat-exchanging component 27 connects, and the preheating material outlet 26 is with the air inlet 28 by being arranged at outside the housing 3
Connecting pipeline 29 connect.
The horizontal reactor of the disclosure is internally provided with axial slideway, and reactor both sides end socket is detachable, in reactor
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 horizontal reactor is particularly suitable for use in the reaction that internal diameter is smaller, barrel lenght is longer
Device structure, solve the problems, such as that operating personnel cannot be introduced into inside reactor and carry out Catalyst packing.In addition, the horizontal reactor
Heat-exchanging component is inside provided with, fresh feed gas enters the preheating material positioned at reactor head after heat-exchanging component raises temperature
Air inlet, improve the material temperature into reactor, reduce reacting product outlet temperature, not only increase energy utilization effect
Rate, also there is the function of regulation reactor self heat balance.
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 housing 3 are attached can be
This area routine, in a kind of embodiment of the disclosure, for the ease of dismounting, the first end socket 5 and the second end socket 4 can
To be sealingly fastened in respectively by first flange 7 and second flange 8 in the left port and right output port of housing 3.
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 horizontal reactor.In a kind of embodiment of the disclosure, urge
Agent bed 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 do not limit, as long as disclosure satisfy that bed pressure drop requirement and the machinery needed for loading catalyst are strong
Spend and do not chemically reacted with material in reaction system, it is preferable that top blind flange 16 and bottom support plate 13 are each only
It is on the spot expanded metal or woven wire.The side wall baffle plate of catalyst bed layer frame 9 is preferably close with the inwall of horizontal reactor
Fitting.
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 respectively used to place catalyst to form beds, and each catalytic reaction unit can be loaded and unloaded individually, easy for installation.
Further, in order to avoid occurring channel, first end catalytic reaction unit 20, the and of interior catalyst reaction member 22 in reactor
It can be brought into close contact between the adjacent side wall of the second end catalytic reaction unit 21.Interior catalyst reaction member 22 can be one
It is individual or be brought into close contact the multiple of setting, preferably 2~8.First end catalytic reaction unit 20 and the second end catalytic reaction list
Member 21 shape preferably according to reactor end socket shape determine, i.e., the shape of end catalyst reaction member outer baffle 19 preferably with
Contact end socket shape it is identical, as shown in Fig. 2, Fig. 3, Fig. 6.First end catalytic reaction unit 20 and the second end catalysis are anti-
Answering the position of unit 21 can be defined by end socket, housing 3 and axial slideway 17；The position of interior catalyst reaction member 22 can
To be defined by housing 3, first end catalytic reaction unit 20, the second end catalytic reaction unit 21 and axial slideway 17.
Further, for the ease of support, first end catalytic reaction unit 20 and the lower section of the second end catalytic reaction unit 21 can be with
First end socket journal stirrup 14 and the second end socket journal stirrup 15 are set respectively.
According to the disclosure, the height of catalyst bed layer frame 9 can be the 0.15~0.95 of horizontal reactor inside diameter
Times, preferably 0.25~0.8 times, most preferably height is 0.5~0.75 times.
According to the disclosure, the shape of housing 3 can be that this area is conventional, and housing and end socket material, thickness can bases
Actual reaction process condition determines.In order to suitable for reaction under high pressure environment, such as when reaction pressure is more than 0.5MPaG, at this
In a kind of disclosed embodiment, as shown in Figure 1-Figure 3, housing 3 can be cylindrical shape or oval cylinder pressure-bearing shell, left
Port and right output port can be that shape is corresponding circular or oval.In another embodiment of the disclosure, example
When the horizontal reactor such as being applied into low pressure reaction environment, as reaction pressure be normal pressure to 0.3MPaG when, such as Fig. 7-Fig. 9 institutes
Show, housing 3 can be rectangular cylinder shape pressure-bearing shell, and left port and right output port are correspondingly rectangle.
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 housing 3 are fixedly connected.Slideway is those skilled in the art
Known, the disclosure does not do any restrictions, as long as the horizontal disengaging housing of catalyst bed layer frame 9 can be realized.It should mend
Explanation is filled, reacting gas should be avoided to occur channel, short circuit phenomenon at slideway.
According to the disclosure, as shown in Fig. 5-Fig. 6, in order to further improve reaction conversion ratio and reaction efficiency in reactor,
Multiple catalyst bed layer frames 9, preferably 2~4 can be arranged at intervals in the housing 3 of the horizontal reactor from top to bottom, each
The 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, heat-exchanging component 27 can be used for improving the material temperature into reactor, reduces reaction product and goes out
Mouth temperature, fresh feed gas are preheated from air inlet 28 into heat-exchanging component 27, and the unstripped gas after preheating passes through connecting pipeline
29 enter preheating material air inlet 1, enter feed surge area 10, catalyst bed layer frame after passing sequentially through the distribution of gas distributor
9 occur chemical reaction, discharging buffering area 11, and after the heat exchange cooling of heat-exchanging component 27, product leaves reactor from gas outlet 2.
In order to further improve heat exchange efficiency, in the disclosure preferably a kind of embodiment, heat-exchanging component 27 can position
In all lower sections of catalyst bed layer frame 9, in the embodiment that reactor includes gas collection grid 12, heat-exchanging component can be located at
In discharging buffering area 11 below the top of gas collection grid 12, all catalyst bed layer frames 9.Form, the size of heat-exchanging component 27
As long as etc. parameter can determine that heat exchange function can be realized according to specific reaction process condition, meet related process, equipment ginseng
The conditions such as number.Heat-exchanging component 27 can be selected from tube heat exchanging component and/or plate type heat exchanging element.Except reactor goes into operation the stage
Outside, during normal reaction device operates, unstripped gas absorbs partial reaction product heat by heat-exchanging component 27, improves and enters reaction
The unstripped gas temperature of device bed, be advantageous to the progress of reaction.Reactor outlet temperature can be controlled by inlet amount, work as reactor
When outlet temperature reduces, unstripped gas inlet amount can be increased to improve bed temperature；, can be with when reactor outlet temperature raises
Reduce unstripped gas inlet amount to reduce bed temperature.
According to the disclosure, reacting gas is sent into for the ease of distribution, in a kind of embodiment of the disclosure, this is sleeping
Formula reactor also includes at least one gas distributor 6, and gas distributor 6 can be arranged at the lower section of preheating material air inlet 1, gas
The number of body distributor 6 is preferably two.
According to the disclosure, the gas containing reaction product is sent out for the ease of concentrating, the horizontal reactor also includes gas collection
Grid 12, 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 horizontal reactor of the disclosure to be included：Urge
Agent bed frame 9 or catalytic reaction unit can take out from the left port at end socket or right output port are horizontal, and from the left side at end socket
Slideway 17 is horizontally placed in the housing 3 vertically for port or right output port.The method of catalyst change can include：As Fig. 4,
Shown in Figure 10, the second end socket 4 connected by second flange 8 is opened, the second end catalytic reaction is extracted out from right output port is sequentially horizontal
Unit 21, interior catalyst reaction member 22 and first end catalytic reaction unit 20, fresh catalyst is changed, then sequentially from the right side
The port horizontally mounted first end catalytic reaction unit 20 for filling fresh catalyst of slideway 17, interior catalyst reaction vertically
Unit 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, horizontal reactor is provided with preheating material gas air inlet including top used by the present embodiment
1, bottom is provided with the cylindrical shape pressure-bearing shell 3 of gas outlet 2, preheating material outlet 26 and air inlet 28, preheating material gas air inlet 1
Bottom is provided with gas distributor 6, and the top of gas outlet 2 is provided with gas collection grid 12, and pipe type heat transfer is provided with the buffering area 11 that discharges
Component 27, it is in fluid communication between preheating material air inlet 1 and preheating material outlet 26 by connecting pipeline 29.The inwall of housing 3 is set
Two axial slideways 17 for being in same level height are equipped with, both sides end socket inwall is provided with supporting base end portion catalytic reaction unit
First end socket journal stirrup 14, the second end socket journal stirrup 15.End catalyst reaction member outer baffle 19, end catalyst reaction member Internal baffle
25th, the first interior catalyst reaction member side wall 23, the second interior catalyst reaction member side wall 24 use percent opening as 5%, hole
Size is 3mm sheet metal, and beds bottom support plate 13 uses the metal that percent opening is 3mm for 35%, hole size
Thin plate, beds top blind flange 16 use woven wire.
A diameter of 750mm, the tangential length 2500mm of housing 3.Catalyst bed layer frame 9 includes 5 interior catalysts and reacted
Unit, 2 end catalyst reaction members are formed, the axial length 500mm of interior catalyst reaction member, width 440mm, height
For 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 horizontal reactor and the contrast situation of axial flow reactor in the prior art of the disclosure.Two kinds anti-
Answer device loaded catalyst, unstripped gas composition and other process conditions it is all identical, from CO conversion ratios, target product selectivity,
The horizontal reactor that four outlet temperature, bed pressure drop indexs can be seen that the disclosure all shows more excellent performance,
Especially advantage is fairly obvious in terms of pressure drop.
The reactor of the embodiment 1 of table 1 contrasts with conventional axial reactor
| Type of reactor | CO conversion ratios/(%) | CH4Selectivity/(%) | Outlet temperature/(DEG C) | Pressure drop/(kPa) |
| Conventional axial reactor | 43 | 95 | 600 | 8.2 |
| The reactor of embodiment 1 | 47 | 94 | 560 | 2.5 |
Flow using the horizontal 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, sequentially horizontal the second end catalytic reaction unit 21,5 interior catalyst reaction members, first ends extracted out urge
Change reaction member 20, replacing fresh catalyst is carried out to catalytic reaction unit.After the completion of replacing, sequentially slideway 17 is horizontal vertically
First end catalytic reaction unit 20,5 interior catalyst reaction members 22, the second ends that introducing fills fresh catalyst are urged
Change reaction member 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, outlet temperature
Four degree, bed pressure drop indexs can be seen that reactor of the present utility model and all show more excellent performance, especially
Advantage is fairly obvious in terms of pressure drop.
The reactor of the embodiment 2 of table 2 contrasts with axial flow reactor
| Type of reactor | CO conversion ratios/(%) | CH4Selectivity/(%) | Outlet temperature/(DEG C) | Pressure drop/(kPa) |
| Conventional axial reactor | 43 | 95 | 600 | 8.2 |
| The reactor of embodiment 1 | 47 | 94 | 560 | 2.5 |
| The reactor of embodiment 2 | 47 | 94 | 565 | 2.3 |
Embodiment 3
As shown in Figure 7, Figure 8, horizontal reactor housing is rectangle used by the present embodiment, and end socket is metal plate, shell
Body size is：2500mm*600mm*600mm, catalyst bed layer frame 9 include 5 interior catalyst reaction members, and end catalyst is anti-
Answer unit identical with interior catalyst reaction member shape and size, therefore be collectively referred to as interior catalyst reaction member herein, inside is urged
Change the axial length 500mm of reaction member, width 600mm, be highly 400mm, as shown in figure 9, interior catalyst reaction member
It 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 horizontal reactor performance indications of the disclosure.After reactor for treatment, VOCs extrusion rates in periodic off-gases
For 100%, from VOCs removal efficiencies, bed pressure drop two indices can be seen that the disclosure reactor show it is more excellent
Performance, advantage is fairly obvious especially in terms of pressure drop.
The horizontal reactor performance indications 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 horizontal reactor more catalyst changeout of the present embodiment is as shown in Figure 10：Opening is connected by second flange 8
The second end socket 4 connect, it is sequentially horizontal to extract 5 interior catalyst reaction members out, carry out changing fresh catalyst operation, catalytic reaction
After the completion of the catalyst change of unit, sequentially slideway 17 is horizontal vertically introduces 5 interior catalysts for filling fresh catalyst
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)
- A kind of 1. horizontal reactor, it is characterised in that the horizontal reactor include housing (3), air inlet (28), gas outlet (2), First end socket (5), the second end socket (4), preheating material air inlet (1), preheating material outlet (26), heat-exchanging component (27), axial direction Slideway (17) and catalyst bed layer frame (9)；The axial slideway (17) is fixed on the housing (3) inside, for slidingly supporting the catalyst bed layer frame (9)；First end socket (5) and the second end socket (4) are removably sealingly fastened in the left port at the housing (3) both ends respectively In right output port, the catalyst bed layer frame (9) slideway (17) level can skid off or slip into the left port or the right side vertically Port；The air inlet (28), preheating material outlet (26) and the gas outlet (2) are located at the bottom of the housing (3), described Preheating material air inlet (1) is located at the top of the housing (3)；The air inlet (28) and preheating material outlet (26) are logical Cross and be arranged at internal heat-exchanging component (27) connection of the housing (3), the preheating material outlet (26) and the air inlet (28) connected by being arranged at the outside connecting pipeline (29) of the housing (3).
- 2. horizontal reactor according to claim 1, it is characterised in that first end socket (5) and the second end socket (4) point It is not sealingly fastened in by first flange (7) and second flange (8) in the left port and right output port of the housing (3).
- 3. horizontal 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 each independently Expanded metal or woven wire, the height of the catalyst bed layer frame (9) are the 0.15 of the horizontal reactor inside diameter ~0.95 times.
- 4. horizontal reactor according to claim 1, it is characterised in that the catalyst bed layer frame (9) include it is horizontal according to First end catalytic reaction unit (20), interior catalyst reaction member (22) and the second end catalytic reaction unit of secondary arrangement (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.
- 5. horizontal reactor according to claim 1, it is characterised in that the housing (3) is cylindrical shape or oval cylinder Pressure-bearing shell, the left port and right output port are circular or ellipse；Or the housing (3) is rectangle tubular pressure-bearing shell Body, the left port and right output port are rectangle.
- 6. horizontal reactor according to claim 1, it is characterised in that the axial slideway (17) includes being set in parallel in The first slideway and the second slideway of same level height, first slideway and second slideway are interior with housing (3) respectively Wall is fixedly connected.
- 7. horizontal reactor according to claim 1, it is characterised in that in the housing (3) of the horizontal reactor from upper and Under be arranged at intervals with 2~4 catalyst bed layer frames (9), being designed with being used for below each catalyst bed layer frame (9) can Slidably support the axial slideway (17) of the catalyst bed layer frame (9).
- 8. horizontal reactor according to claim 1, it is characterised in that the heat-exchanging component (27) described is urged positioned at all Below agent bed frame (9).
- 9. horizontal reactor according to claim 1, it is characterised in that the horizontal reactor also includes gas distributor (6), the gas distributor (6) is arranged at below the preheating material air inlet (1).
- 10. horizontal reactor according to claim 1, it is characterised in that the horizontal reactor also includes gas collection grid (12), the gas collection grid (12) is arranged between the heat-exchanging component (27) and the gas outlet (2).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720810634.2U CN207102556U (en) | 2017-07-05 | 2017-07-05 | Horizontal reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720810634.2U CN207102556U (en) | 2017-07-05 | 2017-07-05 | Horizontal reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110615408A (en) * | 2018-06-19 | 2019-12-27 | 盐城市恒星石油化学有限公司 | Sulfur trioxide conversion process for white oil production |
| CN110615407A (en) * | 2018-06-19 | 2019-12-27 | 盐城市恒星石油化学有限公司 | Conversion process of sulfur trioxide for base oil sulfonation |
| CN112588206A (en) * | 2020-11-27 | 2021-04-02 | 宇部兴产株式会社 | Horizontal multi-process plate type reaction equipment for large-scale DMO reaction |
| CN113620242A (en) * | 2021-08-18 | 2021-11-09 | 西安交通大学 | Gas-transmission type methane/carbon dioxide photo-thermal coupling dry reforming reactor with replaceable catalyst lining plate and using method |
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2017
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110615408A (en) * | 2018-06-19 | 2019-12-27 | 盐城市恒星石油化学有限公司 | Sulfur trioxide conversion process for white oil production |
| CN110615407A (en) * | 2018-06-19 | 2019-12-27 | 盐城市恒星石油化学有限公司 | Conversion process of sulfur trioxide for base oil sulfonation |
| CN110615407B (en) * | 2018-06-19 | 2023-07-07 | 盐城市恒星石油化学有限公司 | Conversion process of sulfur trioxide for sulfonation of base oil |
| CN110615408B (en) * | 2018-06-19 | 2023-08-04 | 盐城市恒星石油化学有限公司 | Sulfur trioxide conversion process for white oil production |
| CN112588206A (en) * | 2020-11-27 | 2021-04-02 | 宇部兴产株式会社 | Horizontal multi-process plate type reaction equipment for large-scale DMO reaction |
| CN113620242A (en) * | 2021-08-18 | 2021-11-09 | 西安交通大学 | Gas-transmission type methane/carbon dioxide photo-thermal coupling dry reforming reactor with replaceable catalyst lining plate and using method |
| CN113620242B (en) * | 2021-08-18 | 2024-03-29 | 西安交通大学 | Methane/carbon dioxide photo-thermal coupling dry reforming reactor with gas permeation type replaceable catalyst lining plate and use method |
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