CN107224938A - A kind of radial reactor - Google Patents
A kind of radial reactor Download PDFInfo
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- CN107224938A CN107224938A CN201610170285.2A CN201610170285A CN107224938A CN 107224938 A CN107224938 A CN 107224938A CN 201610170285 A CN201610170285 A CN 201610170285A CN 107224938 A CN107224938 A CN 107224938A
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- radial direction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0411—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being concentric
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0419—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being placed in separate reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/021—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles comprising a plurality of beds with flow of reactants in parallel
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a kind of radial reactor, including radial direction cylindrical shape seal and pressure bearing housing (1), 1# straight tubes (2), 2# straight tubes (3) and cylindrical shape catalytic reaction unit (4)；Catalytic reaction unit (4) includes central tube (11), radial direction microchannel reaction zone (9) and radial direction catalytic reaction zone (8).Compared with prior art, structure of reactor of the invention is compact, active metal consumption is few, bed pressure drop is small, the gaseous product residence time is short, and bed space availability ratio is high, without gas bias current and short circuit phenomenon.
Description
Technical field
The present invention relates to a kind of radial reactor.
Background technology
Fixed bed reactors mainly have two types, and one kind is axially-located bed reactor, and another is footpath
To fixed bed reactors.Axially-located bed reactor design, process are relatively easy, simple to operate,
But have that reactor apparatus bulky dimensions, bed pressure drop are big, local run aways easily occur, to move heat slow,
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 short in the beds residence time, but reactant difficult to realize being uniformly distributed diametrically,
Easily there is reactant channel or short circuit phenomenon, reduce the overall catalytic perfomance of reactor.
In order to overcome in traditional chemical industry exist heat transfer, mass-transfer efficiency is low the problem of, twentieth century 80 or nine ten years
In generation, has risen micro- Chemical Engineering Technology.Microreactor is as the core component of micro- Chemical Engineering Technology, and it is with milli
Rice, micron are the chemical reaction system of magnitude.One side microreactor has minute yardstick, larger ratio
Surface, the features such as diffusion length is short, the residence time is short, resistance is small, its mass transfer, heat transfer and reaction effect
The 1-3 orders of magnitude high compared with common response device；On the other hand, it can be required according to actual industrial capacity,
It is integrated and increase and decrease of quantity reaches control and regulation production by the microreactor module with functionalization,
The maximum utilization ratio of equipment is advantageously implemented, while shortening the process time of equipment.
In recent years, micro passage reaction gas-solid catalysis, solid super acid reaction in by more next
More concerns.Notification number is CN204841617U, CN204816459U Chinese patent, will be micro-
Channel reactor applies to coal to SNG methanation process, and target product has higher selectivity；It is public
Accuse number Chinese patent for being CN203540513U and disclose a kind of microchannel plate for methanation process
Device is answered, micro- reaction channel is fixed in the supporting plate in the middle part of reactor, it is difficult to eliminate generation of expanding with heat and contract with cold
Stress；Notification number for CN102151531A Chinese patent disclose a kind of micro passage reaction and its
The method of synthesis gas full methanation, the microreactor is by some reaction channels and moves passage of heat alternating parallel
Arrangement, the pressure drop of reactor is larger, while being difficult to bear high pressure.
Therefore, in order to further improve the fluid uniformity of radial reactor, the equipment chi of reactor is reduced
It is very little, improve reaction-ure conversion-age, fully extension catalyst service life, meet reactor maximization
Demand is still technical problem urgently to be resolved hurrily at present, while being also the hair of following radial fixed-bed reactor
Open up direction.
The content of the invention
It is an object of the invention to provide a kind of radial reactor, the reactor catalyst usage amount is few, pressure drop
The low, residence time is short, space availability ratio is high, without gas bias current and short circuit phenomenon.
To achieve these goals, the present invention provides a kind of radial reactor, and the reactor includes radially circle
Shaped seals pressure-bearing shell, the 1# straight tubes for extending into from case top enclosure interior, stretch into from housing bottom
To enclosure interior 2# straight tubes and be arranged on below 1# straight tubes in housing above 2# straight tubes and housing
Coaxial cylindrical shape catalytic reaction unit；By top sealing plate and sealed bottom above and below catalytic reaction unit
Plate is sealed, and annular space is formed between the lateral wall of catalytic reaction unit and the madial wall of housing；Under annular space
End seal is closed and upper end is in fluid communication with 1# straight tubes；During catalytic reaction unit includes central tube and is radially set in
Columnar radial direction microchannel reaction zone and radial direction catalytic reaction zone on heart pipe, radial direction microchannel reaction zone
There is 1# mass flow pathways between radial direction catalytic reaction zone；The upper end of central tube is closed by top sealing plate, under
End is in fluid communication through sealed bottom plate and 2# straight tubes；Radial direction microchannel reaction zone has one or radial direction
Between the multiple radial direction microchannels reaction member being set-located, adjacent two radial direction microchannels reaction member
With 2# mass flow pathways；Have the micro- reaction of multiple radial directions logical on the barrel of each radial direction microchannel reaction member
Only it is in fluid communication inside and outside road, the cylinder of radial direction microchannel reaction member by the micro- reaction channel of radial direction；Footpath
On to the side wall of catalytic reaction zone there is at least one to be used for the sandwich component of containing catalyst bed, the folder
The side wall of layer component is to pass through the stream inside and outside fluid-impermeable structure, and the cylinder of radial direction catalytic reaction zone
The side wall of the permeable sandwich component of body and be in fluid communication.
Preferably, radial direction catalytic reaction zone is located at inner barrel or the outside of radial direction microchannel reaction zone.
Preferably, radially the inner surface of micro- reaction channel is loaded with catalytic active component.
Preferably, radially micro- reaction channel is in conical pipe, flaring pipe, laddertron and Y tube
One of which
Preferably, radially the diameter of micro- reaction channel from the direction of microchannel lateral port side port into microchannel
It is gradually reduced；Radially the diameter of micro- reaction channel is between 2-50 millimeters；The diameter of microchannel lateral port
Ratio with the diameter of side port in microchannel is (1.1-25)：1；In the reaction member of single radial direction microchannel
The cumulative volume of the inner space of multiple micro- reaction channels of radial direction is the barrel of the radial direction microchannel reaction member
The 30%-90% of volume.
Preferably, the dividing plate for axially spaced beds is provided with radial direction catalytic reaction zone, every
The quantity of plate is 2-16.
Preferably, the radially inner side of radial direction catalytic reaction zone intraformational bed component is provided with gas redistribution plate,
The quantity of gas redistribution plate is 1-6.
Preferably, the side wall of the sandwich component in radial direction catalytic reaction zone is Johnson Net.
Preferably, the bottoms of 1# straight tubes be provided with least one be used for be distributed send into the reaction gas of reactor
Gas distributor.
Preferably, heat-barrier material area is provided between the bottom of catalytic reaction unit and the bottom of housing.
The reactor that the present invention is provided is applied to strong exothermal reaction, has strong body before and after the reaction that is particularly suitable for use in
The exothermic reaction of product change.
Compared with prior art, the present invention has advantages below：
1st, radial direction microchannel reaction zone is combined with conventional radial direction catalytic reaction zone, can reaches and carry
The high fluid uniformity, improves feed stock conversion, can reduce again in reactor all using micro- reaction channel
Equipment cost；
2nd, radial direction microchannel reaction zone is made up of some micro- reaction channels of size identical, plays distribution anti-
Answer the effect of material；Dividing plate is set to also play distribution reaction to a certain extent in radial direction catalytic reaction zone
The effect of material；In addition, between radial direction microchannel reaction zone and radial direction catalytic reaction zone and radially be catalyzed
Mass flow pathway between reaction member plays a part of buffering material so that the reactionless dead band of catalytic reaction unit
With the Biased flow phenomenon of gas, the temperature of bed is more uniform, is not in focus, has fully ensured that whole
Even running in the cycle of operation；
3rd, using coating reactivity catalyst in radially micro- reaction channel inner surface, active metal is used
Measure as the 5%-25% of the conventional fixed bed reactors amount used of equal disposal ability, significantly reduce catalysis
Agent production cost；
4th, the residence time is shorter in the reactor for reaction product, extends the service life (longevity of catalyst
Life can improve 15%-40%), bed pressure drop is low compared with the radial reactor of same treating capacity (30%-65%)；
5th, the feed stock conversion of the reactor, target product selectivity are high, unit reactor production intensity
More conventional fixed bed, fluid bed are all high, and when reaching the conversion ratio and product yield under equal conditions, this is anti-
Answer the disposal ability of device bigger (improving 10%-25%)；
6th, for the catalytic reaction of volume-diminished, using the microchannel of coating reactivity catalyst
Reactor, as reactant flows from micro- reaction channel larger diameter end to smaller diameter end, reaction channel is got over
Come smaller, increase volume-diminished and react the motive force converted to product direction, while gas flow rate is more next
It is bigger so that residence time of the gas in micro- reaction channel is shorter, the quilt of the reaction heat of generation also quickly
Take away catalytic reaction unit；For the reaction that volume increases, reactant is smaller straight from micro- reaction channel
Footpath end is flowed to larger diameter end, and reaction channel is increasing, increases volume increase reaction to product direction
The motive force of conversion；
7th, by radial direction catalytic reaction unit and can be had according to actual industrial capacity requirement
The microreactor module of functionalization is integrated and increase and decrease of quantity reaches control and regulation production, is conducive to reality
The maximum utilization ratio of existing equipment, without obvious enlarge-effect, while shortening the process time of equipment, enters one
Step reduction reactor production cost；
8th, it can not only apply to coal system and substitute natural gas and gas employing methanation of coke oven technique, it may also be used for
The fixed-bed catalytic exothermic reaction such as methanol-fueled CLC, F- T synthesis.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with
Following embodiment is used to explain the present invention together, but is not construed as limiting the invention.
In accompanying drawing：
Fig. 1 is a kind of structural representation of the embodiment for the radial reactor that the present invention is provided；
Fig. 2 is a kind of sectional view (i.e. Fig. 1 of the embodiment for the radial reactor that the present invention is provided
The sectional view in middle A-A faces)；
Fig. 3 is the structural representation of another embodiment for the radial reactor that the present invention is provided；
Fig. 4 is that the sectional view of another embodiment for the radial reactor that the present invention is provided (is schemed
The sectional view in A-A faces in 3)；
Fig. 5 is the structural representation of the third embodiment of the radial reactor that the present invention is provided；
Fig. 6 is that the sectional view of the third embodiment of the radial reactor that the present invention is provided (is schemed
The sectional view in A-A faces in 5)；
Fig. 7 is the structural representation of the 4th kind of embodiment of the radial reactor that the present invention is provided；
Fig. 8 is that the sectional view of the 4th kind of embodiment of the radial reactor that the present invention is provided (is schemed
The sectional view in A-A faces in 7)；
Fig. 9 is a kind of specific embodiment party for micro- reaction channel that the radial reactor that the present invention is provided is used
The schematic diagram of formula (conical pipe)；
Figure 10 is a kind of specific implementation for micro- reaction channel that the radial reactor that the present invention is provided is used
The schematic diagram of mode (flaring pipe)；
Figure 11 is a kind of specific implementation for micro- reaction channel that the radial reactor that the present invention is provided is used
The schematic diagram of mode (Y tube)；
Figure 12 is a kind of specific implementation for micro- reaction channel that the radial reactor that the present invention is provided is used
The schematic diagram of mode (laddertron).
Description of reference numerals
The catalytic reaction unit of 1 housing, 2 1# straight tubes, 3 2# straight tubes 4
The radial direction catalytic reaction zone of 5 top sealing plate, 6 sealed bottom plate, 7 annular space 8
The radial direction microchannel reaction member of 9 radial direction microchannel reaction zone 10
Side port in the microchannel of 11 central tube, 12 microchannel lateral port 13
The micro- first gas distributor of reaction channel 16 of the radial direction of 14 1# mass flow pathways 15
The heat-barrier material area of 17 second gas distributor 18
The gas of 19 2# mass flow pathways, 20 dividing plate 21 redistributes plate
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that
Embodiment described herein is merely to illustrate and explain the present invention, and is not limited to this hair
It is bright.
The present invention provides a kind of radial reactor, the reactor include radial direction cylindrical shape seal and pressure bearing housing 1,
The 1# straight tubes 2 of enclosure interior are extend into from the top of housing 1, extend into enclosure interior from the bottom of housing 1
2# straight tubes 3 and it is arranged on the coaxial with housing 1 of the top of 2 lower section 2# straight tubes of 1# straight tubes in housing 13
Cylindrical shape catalytic reaction unit 4；It is close by top sealing plate 5 and bottom above and below catalytic reaction unit 4
Shrouding 6 is sealed, and annular space 7 is formed between the lateral wall of catalytic reaction unit 4 and the madial wall of housing 1；
The lower end closed of annular space 7 and upper end is in fluid communication with 1# straight tubes 2；Catalytic reaction unit 4 includes central tube
11 are catalyzed instead with the columnar radial direction microchannel reaction zone 9 and radial direction being radially set on central tube 11
Area 8 is answered, there is 1# mass flow pathways 14 between radial direction microchannel reaction zone 9 and radial direction catalytic reaction zone 8；In
The upper end of heart pipe 11 is closed by top sealing plate 5, and lower end is flowed through sealed bottom plate 6 and 2# straight tubes 3
Body is connected；Multiple radial directions that radial direction microchannel reaction zone 9 has one or is radially set-located are micro- logical
There is 2# mass flow pathways 19 between road reaction member 10, adjacent two radial direction microchannels reaction member 10；Often
There is the micro- reaction channel 15 of multiple radial directions on the barrel of one radial direction microchannel reaction member 10, it is radially micro-
Only it is in fluid communication inside and outside the cylinder of pathway reaction unit 10 by the micro- reaction channel 15 of the radial direction；Radially urge
Changing on the side wall of reaction zone 8, there is at least one to be used for the sandwich component of containing catalyst bed, the interlayer
The side wall of component is to pass through the stream inside and outside fluid-impermeable structure, and the cylinder of radial direction catalytic reaction zone 8
The side wall of the permeable sandwich component of body and be in fluid communication.
According to the present invention, the fluid uniformity is improved in order to reach, the purpose of feed stock conversion is improved, radially
Catalytic reaction zone 8 can be located at inner barrel or the outside of radial direction microchannel reaction zone 9, as long as ensureing
The flow direction of reactant is first passes through after radial direction microchannel reaction zone 9 by radial direction catalytic reaction zone 8 i.e.
Can, that is, when radial direction catalytic reaction zone 8 is located at the inner barrel of radial direction microchannel reaction zone 9, instead
Answer thing to enter reactor from 1# straight tubes 2, sequentially pass through radial direction microchannel reaction zone 9 and radial direction catalytic reaction
Area 8, reactor is discharged after collecting at central tube 11 through 2# straight tubes 3, and when radial direction catalytic reaction zone 8
When outside the cylinder of radial direction microchannel reaction zone 9, reactant is then from the 2# straight tubes 3 of reactor bottom
Into reactor, sequentially pass through behind radial direction microchannel reaction zone 9 and radial direction catalytic reaction zone 8 through 1# straight tubes
2 discharge reactors.The volume ratio of radial direction catalytic reaction zone 8 and radial direction microchannel reaction zone 9 can be suitable
Any ratio closed.
According to the present invention, the inside of microchannel catalytic reaction member 10 can with hollow, can with solid, as long as
Radially micro- reaction channel 15 can be accommodated.Radial direction catalytic reaction zone 8 is anti-for conventional radial direction catalysis
Unit is answered, raw material enters radial direction catalytic reaction zone 8 by the side wall of radial direction catalytic reaction zone 8, passes through folder
Beds on layer component are reacted, and pass through the side wall stream of radial direction catalytic reaction zone 8 after reaction again
Go out, this process is well known to those skilled in the art, and the present invention is repeated no more, wherein, sandwich component
Quantity can be determined as needed.
According to the present invention, in order that reactor can be used in chemical reaction, the micro- reaction channel 15 of radial direction
Inner surface can be loaded with catalytic active component.Catalytic active component can use those skilled in the art institute
Well known catalytic active component, such as when applying to methanation reaction, catalytic active component can be had
The metals such as nickel, ruthenium and the rhodium of methanation reaction activity；Described load refers to can be by dipping, ion
The methods such as sputtering, coating or filling load to active component by the catalyst containing active component or directly
In micro- reaction channel.Wherein, active metal component coating loading process can use those skilled in the art
The painting method in known two stages of pretreatment and catalyst deposit including metallic matrix.
According to the present invention, radially micro- reaction channel 15 can be selected from conical pipe, flaring pipe, Y shape
One of which in pipe and laddertron (respectively as shown in Fig. 9, Figure 10, Figure 11 and Figure 12)；It is described
Conical pipe, flaring pipe, Y tube and laddertron can use metal material pipe, ceramic material pipe, excellent
Choosing is using the metal tube not reacted with the gas in reaction system.It should be noted that this area skill
The conventional use of conical pipe of art personnel refers to that the truncated cone-shaped hollow material of both ends open, rather than axial cross section are
The section bar of taper.
According to the present invention, in order to ensure the efficiency of chemical reaction, radially the diameter of micro- reaction channel 15 can
With between 2-50 millimeters.When applying to the reaction of cumulative volume diminution, the micro- reaction channel 15 of radial direction
Diameter can into microchannel, the direction of side port 13 be gradually reduced and (ensures micro- logical from microchannel lateral port 12
The diameter of road lateral port 12 is more than the diameter of side port 13 in microchannel, also first subtracts including channel diameter
Small rear constant situation).The ratio of the diameter of side port 13 in the diameter of microchannel lateral port 12 and microchannel
Value can be (1.1-25)：1, be preferably (2-10)：1.
According to the present invention, the reactor, which applies to react front and rear volume, the exothermic reaction of strong variations, is
The temperature control of reaction efficiency and reactor is taken into account, described in single radial direction microchannel reaction member 10
The cumulative volume of the inner space of multiple micro- reaction channels 15 of radial direction is the radial direction microchannel reaction member 10
The 30%-90% of barrel volume, preferably 40%-65%.
According to the present invention, in order to further improve uniform point in radial direction catalytic reaction zone 8 of reaction mass
The dividing plate 20 for axially spaced bed, dividing plate 20 can be provided with cloth, radial direction catalytic reaction zone 8
Quantity be 2-64, further, it is preferable to which quantity is 2-16, dividing plate 20 is sealingly fastened in bottom
Sealing plate 6 and top sealing plate 5.Gas redistribution plate is also provided with radial direction catalytic reaction zone 8
21, the quantity of gas redistribution plate 21 is 1-25, further, it is preferable to which quantity is 1-6.
According to the present invention, in order to further improve being uniformly distributed for reaction mass, gas redistribution plate 21
On can be provided with size identical gas distribution holes.It should be noted that those skilled in the art often say
Gas distribution holes, can be square hole, slot, circular port, slotted eye, bellmouth etc.
Well format.
According to the present invention, gas redistribution plate 21, dividing plate 20 can use metal material or ceramic material,
It is preferred to use the metal material not reacted with the gas in reaction system.
According to the present invention, the side wall of the sandwich component in radial direction catalytic reaction zone 8 can be about the inferior net of writing brush,
The Johnson Net is well-known to those skilled in the art, and the present invention is repeated no more.
According to the present invention, the bottoms of 1# straight tubes 2 can be provided with least one be used for be distributed feeding it is described instead
Answer the gas distributor of the reaction gas of device.Gas distributor can routinely be made using those skilled in the art
, the present invention repeats no more, and gas distributor is preferably provided with two.
According to the present invention, in order to prevent that the bottom of housing 1 is excessively heated and prevents catalytic reaction unit 4
Move down, heat-barrier material can be provided between the bottom of catalytic reaction unit 4 and the bottom of housing 1
Area 18.Single material or many well-known to those skilled in the art can be placed with heat-barrier material area 18
Plant the heat-barrier materials such as heat insulating ball, heat-insulated felt rug or the heat insulating belt of composite.
The present invention is further illustrated by embodiment below in conjunction with accompanying drawing, not therefore but the present invention
And it is any way limited.
Embodiment 1
As shown in figure 1, the radial reactor that is used of the present embodiment include upper end provided with 1# straight tubes 2, under
Pressure-bearing shell 1 of the end provided with 2# straight tubes 3, the bottom of 1# straight tubes 2 is provided with first gas distributor 16, the
The lower section of one gas distributor 16 is provided with second gas distributor 17.In housing 1 under 1# straight tubes 2
Side has central tube 11, radial direction catalytic reaction zone 8 and radial direction microchannel reaction zone 9, radial direction microchannel plate
Area 9 is answered to include a radial direction microchannel reaction member 10.Radial direction microchannel reaction zone 9, which is arranged on, radially urges
Outside the cylinder for changing reaction zone 8, the side wall of radial direction microchannel reaction member 10 and the madial wall of housing 1
Annular space 7 is formed with, 1# is formed between radial direction catalytic reaction zone 8 and radial direction microchannel reaction member 10
The bottom surface of mass flow pathway 14, radial direction catalytic reaction zone 8 and radial direction microchannel reaction member 10 and housing 1 it
Between be provided with the heat-barrier material area 18 being made up of heat-insulated felt rug.As shown in Fig. 2 the radial direction microchannel plate
Unit 10 is answered to include active by 24900 (to clearly show that, being not entirely shown) inner surface coatings
The micro- reaction channel 15 of radial direction of catalyst, radially micro- reaction channel 15 is using conical pipe as shown in Figure 9.
There are 2 to be used for the sandwich component of containing catalyst bed, radially on the side wall of radial direction catalytic reaction zone 8
Dividing plate 20, the 2 gas redistribution plates 21 of 4 even partition beds are provided with catalytic reaction zone 8,
The radial direction spacing of gas redistribution plate 21 is 85mm, the internal layer gas redistribution distance center pipe 11 of plate 21
Radial direction spacing be 35mm.
The height of radial direction catalytic reaction zone 8 and radial direction microchannel reaction member 10 is 1000mm, housing 1
Internal diameter be 900mm, a diameter of 150mm of central tube 11, the spacing of annular space 7 is 35mm, 1#
The spacing of mass flow pathway 14 is 15mm, the micro- reaction of conical pipe that radial direction microchannel reaction member 10 is used
The length of passage is a diameter of at a diameter of 10mm at 100mm, conical pipe lateral port, interior side port
Cumulative volume inside 4mm, all micro- reaction channels of conical pipe accounts for the body of radial direction microchannel reaction member 10
Long-pending ratio is 44.3%, and the thickness of bed layer of radial direction catalytic reaction zone 8 is 225mm.
The reactor of the present embodiment is applied to table in synthesis gas methanation reaction, the micro- reaction channel of conical pipe
Face supported active metals NiO amount is 9.5g/m2.Synthesis gas enters reactor from 1# straight tubes 2, radially
Through after catalytic reaction unit, collect in central tube 11, discharged from the 2# straight tubes 3 of reactor bottom
Reactor.Unstripped gas H2/ CO volume ratios are 3.02, and reaction temperature is 650 DEG C, and pressure is 3.35MPa,
Volume space velocity is 10038h-1。
What is provided in table 1 is the reactor and the contrast situation of radial reactor in the prior art of the present embodiment.
Two kinds of reactor catalysis reaction members have identical size, from feed stock conversion, the bed uniformity, target
The selectivity of product, service life, bed pressure drop and active metal Ni six indexs of consumption can be with
Find out, reactor proposed by the present invention all shows more excellent performance.
The reactor of the present embodiment of table 1 is contrasted with radial reactor of the prior art
Embodiment 2
As shown in Figure 3, Figure 4, the housing inner diameter of the reactor of the reactor of the present embodiment and embodiment 1,
The structural parameters such as catalytic reaction cell height are identical.Difference from Example 1 is, in the present embodiment
Some radial direction microchannels reaction zone 9 includes two radial direction microchannel reaction members 10.The present embodiment is using such as
Include 44850 in the micro- reaction channel of flaring pipe shown in Figure 10, two radial direction microchannel reaction members 10
The micro- reaction of flaring pipe that inner surface is coated with active catalyst (to clearly show that, is not entirely shown) in root
Passage.In addition, being redistributed in the reactor of the present embodiment in radial direction catalytic reaction zone 8 using 1 gas
Plate 21, the radial direction spacing of the gas redistribution distance center pipe 11 of plate 21 is still 35mm.
The height of radial direction catalytic reaction zone 8 and radial direction microchannel reaction member 10 is 1000mm, housing 1
Internal diameter be 900mm, a diameter of 150mm of central tube 11, the spacing of annular space 7 is 35mm, 1#
The spacing of mass flow pathway 14 is 15mm, and the spacing of 2# mass flow pathways 19 is 15mm, and radial direction microchannel plate should
The length for the micro- reaction channel of flaring pipe that unit 10 is used is 67.5mm, at flaring pipe lateral port
A diameter of 10mm, a diameter of 4mm at interior side port, inside all micro- reaction channels of flaring pipe
The ratio that cumulative volume accounts for the volume of radial direction microchannel reaction zone 9 is 42.9%, radial direction catalytic reaction zone 8
Thickness of bed layer is 175mm.
The radial reactor can be equally used for methanation reaction.According to reaction condition same as Example 1,
The conversion ratio of gained carbon monoxide is 73.5%, and the selectivity of methane is 98%.
Embodiment 3
As shown in Figure 5, Figure 6, the housing inner diameter of the reactor of the reactor of the present embodiment and embodiment 1,
The structural parameters such as catalytic reaction cell height are identical.Difference from Example 1 is, the present embodiment
Radial direction catalytic reaction zone 8 and the position of radial direction microchannel reaction zone 9 are exchanged in reactor, and 1# straight tubes 2
Bottom be not provided with gas distributor.In addition, in radial direction catalytic reaction zone 8 in the reactor of this example
Plate 21 is redistributed using 2 gases, the spacing of two gas redistribution plates 21 is 60mm, innermost layer
It is 30mm that gas, which redistributes plate and the radial direction spacing of the madial wall of radial direction catalytic reaction zone 8,.
The reactor that the present embodiment is used can be applied to synthesis gas and synthesize C in Fe bases catalyst2、C3Etc. small
Molecular olefine.Supported active metals Fe amounts are 10.5g/m in conical pipe2.Synthesis gas is from reactor bottom
2# straight tubes 3 enter reactor, collect in central tube 11, after catalytic reaction unit,
Reactor is discharged from 1# straight tubes 2.Unstripped gas H2/ CO volume ratios are 2, and reaction temperature is 320 DEG C, pressure
Power is 0.5MPa, and volume space velocity is 3500h-1。
What is provided in table 2 is the reactor and the contrast situation of radial reactor in the prior art of the present embodiment.
Two kinds of reactor catalysis reaction members have identical size, from feed stock conversion, the bed uniformity, target
The selectivity of product, service life, bed pressure drop and active metal Fe six indexs of consumption can be with
Find out, reactor proposed by the present invention all shows more excellent performance.
The reactor of the present embodiment of table 2 is contrasted with radial reactor of the prior art
Embodiment 4
As shown in Figure 7, Figure 8, the reactor shell internal diameter of the present embodiment reactor and embodiment 3, urge
Change the structural parameters such as reaction member height identical.It is with the difference of embodiment 3, the radial direction is urged
Change and gas redistribution plate 21 is not provided with reaction zone 8.
The reactor of the present embodiment can be applied to synthesis gas in Cu base catalyst synthesizing methanols, and unstripped gas is from anti-
Answer the 2# straight tubes 3 of device bottom to enter, radially across catalytic reaction unit, reaction is left from 1# straight tubes 2
Device.Supported active metals Cu amount is in the micro- reaction channel of conical pipe in the reactor of the present embodiment
18g/m2.Unstripped gas H2/ CO volume ratios are 2, and reaction temperature is 245 DEG C, and pressure is 5.5MPa, body
Product air speed is 3000h-1.One way CO conversion ratios are 8.6%, and methanol selectivity is 99.5%, bed pressure
Drop is lower than conventional radial reactor by 38%.
Radial reactor compact conformation that the present invention is provided, active metal consumption is few, bed pressure drop is small, gas
The body product residence time is short, and bed space availability ratio is high, without gas bias current and short circuit phenomenon.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited
Detail in above-mentioned embodiment, can be to the present invention in the range of the technology design of the present invention
Technical scheme carry out a variety of simple variants, these simple variants belong to protection scope of the present invention.
In addition, various embodiments of the present invention can be combined randomly, as long as its
Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of radial reactor, it is characterised in that the reactor includes radial direction cylindrical shape seal and pressure bearing
Housing (1), the 1# straight tubes (2) that enclosure interior is extend at the top of the housing (1), from the shell
Body (1) bottom extend into the 2# straight tubes (3) of enclosure interior and is arranged on the interior institute of the housing (1)
State the cylindrical shape catalysis coaxial with housing (1) above the 2# straight tubes (3) below 1# straight tubes (2)
Reaction member (4)；By top sealing plate (5) and sealed bottom plate above and below catalytic reaction unit (4)
(6) seal, be formed between the lateral wall of catalytic reaction unit (4) and the madial wall of housing (1)
Annular space (7)；The lower end closed of annular space (7) and upper end and the 1# straight tubes (2) fluid communication；Catalysis
Reaction member (4) includes central tube (11), the columnar footpath being radially set on central tube (11)
To microchannel reaction zone (9) and radial direction catalytic reaction zone (8), radial direction microchannel reaction zone (9) and footpath
To between catalytic reaction zone (8) have 1# mass flow pathways (14)；The upper end of central tube (11) is by the top
Portion's sealing plate (5) is closed, and lower end is flowed through the sealed bottom plate (6) with the 2# straight tubes (3)
Body is connected；It is multiple that radial direction microchannel reaction zone (9) is set-located with one or radially
Have between radial direction microchannel reaction member (10), adjacent two radial direction microchannels reaction member (10)
2# mass flow pathways (19)；There are multiple radial directions on the barrel of each radial direction microchannel reaction member (10)
It is only radially micro- by this inside and outside micro- reaction channel (15), the cylinder of radial direction microchannel reaction member (10)
Reaction channel (15) is in fluid communication；Have at least one on the side wall of the radial direction catalytic reaction zone (8)
The individual sandwich component for containing catalyst bed, the side wall of the sandwich component is fluid-impermeable structure,
And the inside and outside sandwich component by the fluid-impermeable of the cylinder of the radial direction catalytic reaction zone (8)
Side wall and be in fluid communication.
2. reactor according to claim 1, wherein, the radial direction catalytic reaction zone (8) is located at institute
State inner barrel or the outside of radial direction microchannel reaction zone (9).
3. reactor according to claim 1, wherein, the micro- reaction channel of radial direction (15) it is interior
Area load has catalytic active component.
4. reactor according to claim 1, wherein, the micro- reaction channel of radial direction (15) is choosing
One of which from conical pipe, flaring pipe, laddertron and Y tube.
5. reactor according to claim 1, wherein, the micro- reaction channel of radial direction (15) it is straight
From microchannel lateral port (12), the direction of side port (13) into microchannel is gradually reduced in footpath；The radial direction
The diameter of micro- reaction channel (15) is between 2-50 millimeters；The microchannel lateral port (12) it is straight
The ratio of footpath and the diameter of side port (13) in microchannel is (1.1-25)：1；Single radial direction microchannel plate
The cumulative volume for answering the inner space of multiple micro- reaction channels of radial direction (15) described in unit (10) is the footpath
To the 30%-90% of the barrel volume of microchannel reaction member (10).
6. reactor according to claim 1, wherein, set in the radial direction catalytic reaction zone (8)
There is the dividing plate (20) for axially spaced beds, the quantity of the dividing plate (20) is 2-16.
7. reactor according to claim 1, wherein, it is described in the radial direction catalytic reaction zone (8)
The radially inner side of sandwich component is provided with gas redistribution plate (21), the gas redistribution plate (21)
Quantity be 1-6.
8. reactor according to claim 1, it is characterised in that the radial direction catalytic reaction zone (8)
In sandwich component side wall be Johnson Net.
9. reactor according to claim 1, wherein, the bottoms of the 1# straight tubes (2) be provided with to
Few one is used for the gas distributor that the reaction gas of the reactor is sent into distribution.
10. reactor according to claim 1, wherein, the bottom of the catalytic reaction unit (4)
Heat-barrier material area (18) is provided between the bottom of the housing (1).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109045947A (en) * | 2018-09-03 | 2018-12-21 | 青岛科技大学 | A kind of fluidized bed cluster reactor |
| CN109499262A (en) * | 2018-12-14 | 2019-03-22 | 青岛科技大学 | A kind of novel longitudinal parallel bed adsorption device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87103900A (en) * | 1987-05-27 | 1988-12-14 | 唐国平 | Improved isothermal reaction furnace |
| CN204841618U (en) * | 2015-08-04 | 2015-12-09 | 中国石化工程建设有限公司 | Methanization reactor |
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2016
- 2016-03-23 CN CN201610170285.2A patent/CN107224938B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87103900A (en) * | 1987-05-27 | 1988-12-14 | 唐国平 | Improved isothermal reaction furnace |
| CN204841618U (en) * | 2015-08-04 | 2015-12-09 | 中国石化工程建设有限公司 | Methanization reactor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109045947A (en) * | 2018-09-03 | 2018-12-21 | 青岛科技大学 | A kind of fluidized bed cluster reactor |
| CN109045947B (en) * | 2018-09-03 | 2021-08-17 | 青岛科技大学 | Fluidized bed cluster reactor |
| CN109499262A (en) * | 2018-12-14 | 2019-03-22 | 青岛科技大学 | A kind of novel longitudinal parallel bed adsorption device |
| CN109499262B (en) * | 2018-12-14 | 2021-08-13 | 青岛科技大学 | Novel longitudinal parallel bed adsorber |
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