CN107398238A - A kind of isothermal reactor - Google Patents
A kind of isothermal reactor Download PDFInfo
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- CN107398238A CN107398238A CN201610342292.6A CN201610342292A CN107398238A CN 107398238 A CN107398238 A CN 107398238A CN 201610342292 A CN201610342292 A CN 201610342292A CN 107398238 A CN107398238 A CN 107398238A
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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
- B01J8/0242—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 flow within the bed being predominantly vertical
- B01J8/025—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 flow within the bed being predominantly vertical in a cylindrical shaped bed
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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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated 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
- B01J8/0285—Heating or cooling the reactor
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
- B01J2219/00835—Comprising catalytically active material
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00851—Additional features
- B01J2219/00869—Microreactors placed in parallel, on the same or on different supports
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00873—Heat exchange
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00891—Feeding or evacuation
- B01J2219/00894—More than two inlets
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Abstract
The invention discloses a kind of isothermal reactor, the reactor includes radial direction cylindrical shape seal and pressure bearing housing (1), 1# pipes (9), 2# pipes (11), catalytic reaction zone and the heat transmission equipment for being exchanged heat with the catalytic reaction zone；The catalytic reaction zone includes at least one cylinder (12), multiple micro- reaction channels (6) axially across the cylinder (12) are provided with each described cylinder (12), the guiding subassembly (5) of increase Hydrodynamic turbulence effect is provided with micro- reaction channel (6).Reactor catalyst active component usage amount is few, pressure drop is low, the product residence time is short, feed stock conversion is high for this, without gas bias current and bed temperature runaway phenomenon.
Description
Technical field
The present invention relates to a kind of isothermal reactor.
Background technology
Fixed bed reactors mainly have two types, and one kind is axially-located bed reactor, and another kind is radial fixed-bed
Reactor.Axially-located bed reactor design, process are relatively easy, simple to operate, but reactor apparatus size Pang be present
Greatly, bed pressure drop is big, local run aways easily occurs, moves the problems such as heat is slow, conversion ratio is low, enlarge-effect is obvious.Radial bed is anti-
Answer that device 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 is radially
On be uniformly distributed, the production intensity of unit catalyst bed it is relatively low.
The problem of heat transfer, mass-transfer efficiency is low in traditional chemical industry be present to overcome, twentieth century the 80s and 90s rises
Micro- Chemical Engineering Technology.Core component of the microreactor as micro- Chemical Engineering Technology, it is anti-as the chemistry of magnitude using millimeter, micron
Answer system.One side microreactor has minute yardstick, larger ratio surface, diffusion length is short, the residence time is short, resistance is small etc.
Feature, its mass transfer, heat transfer and reaction effect 1~3 order of magnitude high compared with common response device；On the other hand, can be according to the work of reality
The requirement of industry production capacity, is integrated by the microreactor module with functionalization and the increase and decrease of quantity reaches control and regulation is given birth to
Production, is advantageously implemented the maximum utilization ratio of equipment, while shorten the process time of equipment.
In recent years, micro passage reaction is more and more closed in gas-solid catalysis, solid super acid reaction
Note.Notification number is that CN202893334U Chinese patent discloses a kind of micro passage reaction, and the micro passage reaction uses titanium
Alloy plate type structure, cooling storehouse and reaction warehouse is provided with each titanium alloy cooling cover plate, the micro passage reaction can be born
High pressure and corrosion stability, it is disadvantageous in that reactant residence time in reaction warehouse is short, production efficiency is relatively low.Notification number is
CN203540513U Chinese patent discloses a kind of micro passage reaction for methanation process, and the reactor is by micro- reaction
Passage is fixed in the supporting plate in the middle part of reactor, it is difficult to eliminates the caused stress that expands with heat and contract with cold.Notification number is
CN102151531A Chinese patent discloses a kind of method of methanator and its synthesis gas full methanation, and this is micro- anti-
Device is answered by some reaction channels and moves the arrangement of passage of heat alternating parallel, the pressure drop of reactor is larger, while is difficult to bear high pressure.It is public
Number Chinese patent for being CN204841617U, CN204816459U is accused, methanator is applied into coal to SNG methane chemical industry
Skill, target product have higher selectivity, are disadvantageous in that unstripped gas is shorter in the residence time of such reactor, cause
Feed stock conversion is relatively low.
Therefore, reduce the equipment size of reactor, reduce droop loss, the ditch for avoiding raw material from occurring in beds
Stream and short circuit phenomenon, the transformation efficiency of reactant is improved, the service life of abundant extension reactor, meets reactor maximization
Demand is technical problem urgently to be resolved hurrily at present.
The content of the invention
It is an object of the invention to provide a kind of isothermal reactor, and the reactor catalyst active component usage amount is few, pressure drop
It is low, the product residence time is short, feed stock conversion is high, without gas bias current and bed temperature runaway phenomenon.
To achieve these goals, the present invention provides a kind of isothermal reactor, it is characterised in that：The reactor is included radially
Cylindrical shape seal and pressure bearing housing, the 1# pipes for extending into from the case top enclosure interior, from the housing bottom it extend into shell
The 2# pipes in internal portion, be arranged on catalytic reaction zone in the housing below the 1# pipes above the 2# pipes and for
The heat transmission equipment of the catalytic reaction zone heat exchange；The catalytic reaction zone includes at least one cylinder, the cylinder and the shell
Body is coaxial, and the medial surface of the lateral surface of the cylinder and the housing is inconsistent or coincide；Between two neighboring cylinder, most
Formed with space between the cylinder of lower section and the bottom surface of housing；It is provided with each described cylinder multiple axially across the post
Micro- reaction channel of body, only pass through micro- reaction channel between the 1# pipes and uppermost space and between two neighboring space
It is in fluid communication, the space of bottom and the 2# fluid communications；Increase Hydrodynamic turbulence is provided with micro- reaction channel to make
Guiding subassembly.
Preferably, it has been collectively forming in each described cylinder by each inwall of the cylinder and the outer wall of each micro- reaction channel
One cylinder chamber；The heat transmission equipment is included at least one set on the housing corresponding to the side of each cylinder
The heat transferring medium entrance and heat transferring medium that are located remotely from each other are exported, the heat transferring medium entrance by the cylinder chamber with it is described
Heat transferring medium communication.
Preferably, the interior heat collecting device is included in what is set on the housing corresponding to the side in space each described
At least one pair of heat transferring medium entrance being located remotely from each other, heat transferring medium outlet and the heat exchanger assembly through space, the heat exchange are situated between
Matter entrance by the heat exchanger assembly and the heat transferring medium communication, the heat exchanger assembly be selected from tubular around
At least one of tubulation line, ring-type coiling pipeline, plate-like coiling pipeline and heat exchanger plates.
Preferably, the quantity of the cylinder is 2-500.
Preferably, the guiding subassembly includes the fixing axle being fixedly connected with micro- reaction channel and is connected on described solid
Diversion member on dead axle, one end of the diversion member towards micro- reaction channel airintake direction is convex.
Preferably, the diversion member is selected from solid cone, hollow centrum, circular conical surface, hemisphere, hemisphere face, ball
At least one of body and sphere.
Preferably, the basal diameter of the solid cone, hollow centrum and circular conical surface is less than the downside of micro- reaction channel
The diameter of opening and the greater in the diameter of upper side opening；The hemisphere, hemisphere face, the spherical diameter of sphere and spheroid are small
The diameter of open lower side in micro- reaction channel and the greater in the diameter of upper side opening；The two neighboring diversion member
Spacing is not less than the height of the diversion member.
Preferably, each guiding subassembly includes the 3-100 diversion members.
Preferably, the inner surface of micro- reaction channel and/or the outer surface of diversion member are loaded with catalytic active component.
Preferably, micro- reaction channel is the one of which in conical pipe, flaring pipe, Y tube and laddertron；
The diameter of micro- reaction channel is between 2-50 millimeters；The ratio of the diameter of the upper side opening and the diameter of open lower side is
(0.04-25)：1；The cumulative volume of the inner space of micro- reaction channel is the 30%-90% of the cumulative volume of all cylinders.
Compared with prior art, the present invention has advantages below：
1st, the guiding subassembly of increase Hydrodynamic turbulence effect, and guiding subassembly and micro- reaction channel are provided with micro- reaction channel
Coaxially, turbulent extent of the reaction raw materials in microchannel is added, improves the probability that raw material is acted on catalyst activity position,
So as to improve feed stock conversion；
2nd, the reaction zone that the reactor is made up of some micro- reaction channels of size identical, reactionless dead band and gas it is inclined
Flow phenomenon, heat transmission equipment can remove or provide rapidly the heat needed for reaction, and the temperature of bed is more uniform, is not in heat
Point, the even running in the whole service cycle is fully ensured that；
3rd, for the catalytic reaction of volume-diminished, using coating reactive component micro passage reaction, with
Reactant flows from micro- reaction channel larger diameter end to smaller diameter end, and reaction channel is less and less, increases volume-diminished
The motive force converted to product direction is reacted, while flow velocity is increasing so that residence time of the product in micro- reaction channel
It is shorter, caused reaction heat also quickly be brought away from catalytic reaction zone；For the reaction of volume increase, reactant is from micro- anti-
Passage smaller diameter end is answered to be flowed to larger diameter end, reaction channel is increasing, increases catalytic reaction and turns to product direction
The motive force of change；
4th, made using coating reactive component in the outer surface of microchannel inner surface and/or diversion member, active metal
Dosage is the 1%-35% of equal disposal ability routine fixed bed reactors amount used, has saved the usage amount of active metal, special
The production cost of noble metal catalyst can not reduced；
5th, diffusional resistance of the reactant between bodies of fluid to catalytic active site is almost nil, improves reaction rate,
The product of generation can be diffused into bodies of fluid quickly simultaneously, and the residence time is shorter in the reactor for product, extends catalyst
Service life (life-span can improve 15%-60%), axial flow reactor low (30%- of the bed pressure drop compared with same treating capacity
90%)；
6th, can according to the industrial capacity requirement of reality, by the microreactor module with functionalization it is integrated and
The increase and decrease of quantity reaches control and regulation production, is advantageously implemented the maximum utilization ratio of equipment, without obvious enlarge-effect, simultaneously
Shorten the process time of equipment, further reduce reactor production cost.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of structural representation of embodiment of reactor provided by the invention；
Fig. 2 is the structural representation of another embodiment of reactor provided by the invention；
Fig. 3 is the structural representation of the third embodiment of reactor provided by the invention；
Fig. 4 is the structural representation of the 4th kind of embodiment of reactor provided by the invention；
Fig. 5 is a kind of sectional view of embodiment of reactor provided by the invention (i.e. in Fig. 1, Fig. 2, Fig. 3, Fig. 4
The sectional view in A-A faces)；
Fig. 6 is a kind of sectional view (the B-B faces i.e. in Fig. 3, Fig. 4 of embodiment of reactor provided by the invention
Sectional view)；
Fig. 7 is a kind of used microchannel with guiding subassembly of embodiment of reactor provided by the invention
Schematic diagram；
Fig. 8 is the sectional view (i.e. the sectional view in C-C faces in Fig. 7) of the micro- reaction channel of conical pipe provided by the invention；
Fig. 9 is the sectional view (i.e. the sectional view in D-D faces in Fig. 7) of the micro- reaction channel of conical pipe provided by the invention；
Figure 10 is a kind of embodiment (conical pipe) of micro- reaction channel used by reactor provided by the invention
Schematic diagram；
Figure 11 is that a kind of embodiment of micro- reaction channel used by reactor provided by the invention is (tubaeform
Pipe) schematic diagram；
Figure 12 is a kind of embodiment (Y tube) of micro- reaction channel used by reactor provided by the invention
Schematic diagram；
Figure 13 is a kind of embodiment (laddertron) of micro- reaction channel used by reactor provided by the invention
Schematic diagram；
Figure 14 is that a kind of embodiment (hemisphere) of guiding subassembly used by the reactor that invention provides shows
It is intended to；
A kind of embodiment (hemisphere face) of guiding subassembly shows used by Figure 15 reactors provided by the invention
It is intended to；
The signal of a kind of embodiment (sphere) of guiding subassembly used by Figure 16 reactors provided by the invention
Figure；
The signal of a kind of embodiment (spheroid) of guiding subassembly used by Figure 17 reactors provided by the invention
Figure；
A kind of embodiment (solid cone) of guiding subassembly used by Figure 18 reactors provided by the invention
Schematic diagram；
A kind of embodiment (circular conical surface) of guiding subassembly shows used by Figure 19 reactors provided by the invention
It is intended to；
A kind of embodiment (conulite) of guiding subassembly used by Figure 20 reactors provided by the invention
Schematic diagram.
Description of reference numerals
The cylinder top sealing plate of 1 housing, 2 first gas distributor 3
5 guiding subassembly of side opening, 6 micro- reaction channel on 4
The 1# of 7 open lower side, 8 space 9 is managed
The cylinder of 10 heat-barrier material area, 11 2# pipes 12
The heat exchanger assembly of 13 14 second gas distributor of cylinder sealed bottom plate 15
The diversion member of 16 fixing axle 17
Embodiment
The embodiment of the present invention 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 explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of isothermal reactor, and the reactor includes radial direction cylindrical shape seal and pressure bearing housing 1, from the shell
The top of body 1 extend into the 1# pipes 9 of enclosure interior, the 2# pipes 11 of enclosure interior extend into from the bottom of housing 1, it is described to be arranged on
The catalytic reaction zone of the lower section of the 1# pipes 9 top of 2# pipes 11 and for being exchanged heat with the catalytic reaction zone in housing 1
Heat transmission equipment；The catalytic reaction zone includes at least one cylinder 12, and the cylinder 12 and the housing 1 are coaxial, and the post
The medial surface of the lateral surface of body 12 and the housing 1 is inconsistent or coincides；Between two neighboring cylinder 12, the cylinder of bottom
Formed with space 8 between 12 and the bottom surface of housing 1；It is provided with each described cylinder 12 multiple axially across the cylinder 12
Micro- reaction channel 6, it is only logical by micro- reaction between the 1# pipes 9 and uppermost space 8 and between two neighboring space 8
Road 6 is in fluid communication, and the space 8 of bottom is in fluid communication with the 2# pipes 11；Increase fluid is provided with micro- reaction channel 6
The guiding subassembly 5 of turbulence effect.
According to a kind of embodiment of the present invention, by each inwall of the cylinder 12 and each in each described cylinder 12
The outer wall of micro- reaction channel 6 has been collectively forming a cylinder chamber；The heat transmission equipment can be included in corresponding to each post
At least one pair of heat transferring medium entrance being located remotely from each other and the heat transferring medium outlet set on the housing 1 of the side of body 12, institute
State heat transferring medium entrance and pass through the cylinder chamber and the heat transferring medium communication.Another according to the present invention has
Body embodiment, the heat transmission equipment, which can be included on the housing 1 corresponding to the side in space each described 8, to be set
At least one pair of heat transferring medium entrance being located remotely from each other, heat transferring medium outlet and the heat exchanger assembly 15 through space 8, it is described to change
For thermal medium entrance by the heat exchanger assembly 15 and the heat transferring medium communication, the heat exchanger assembly 15 is choosing
From at least one of tubular coiling pipeline, ring-type coiling pipeline, plate-like coiling pipeline and heat exchanger plates.For strong exothermal reaction
Speech, reaction heat can be removed in time using heat transmission equipment, to reduce bed temperature, improve feed stock conversion；For the endothermic reaction
For, the heat needed for reaction can be provided rapidly using heat transmission equipment, reach the purpose for improving reaction rate.Need what is illustrated
It is that can be in fluid communication between same heat exchanging medium inlet and heat transferring medium outlet by multiple heat exchanger assemblies.
According to the present invention, the cylinder 12 can be made up of upper sealing panel and lower sealing plate, and its side wall can be with the portion of housing 1
Divide side wall to overlap, can also be tightly connected with the side wall of housing 1.Can be with hollow in cylinder 12, can be with solid, as long as can accommodate
Micro- reaction channel 6.
According to the present invention, under identical reaction condition and reactor diameter, the quantity of increase cylinder 12 can increase instead
The time of contact of gas and catalytic active center is answered, improves the effect of conversion ratio, therefore can be adjusted according to real reaction situation
The quantity of whole cylinder 12, the quantity of the cylinder 12 can be 2-500, preferably 5-50.
According to the present invention, in order to improve the conversion ratio of unstripped gas, it is rapid that increase fluid is provided with micro- reaction channel 6
The guiding subassembly 5 of action, the guiding subassembly 5 include fixing axle 16 and diversion member 17.Guiding subassembly 5 and micro- reaction channel 6
Coaxially, the both ends of guiding subassembly 5 are individually fixed in the upper side opening 4 of micro- reaction channel 6, open lower side 7, and the series connection of diversion member 17 is solid
It is scheduled in fixing axle 16, as shown in Fig. 7, Fig. 8, Fig. 9.The size of diversion member 17 that same guiding subassembly 5 uses can be from
The upper side opening 4 of micro- reaction channel 6 is gradually reduced to open lower side 7, can also gradually be increased, can also be constant, preferable same
The size of diversion member 17 that one guiding subassembly 5 uses is identical.Direction micro- airintake direction of reaction channel 6 of diversion member 17
One end is convex, such as can be in hemisphere, hemisphere face, sphere, spheroid, solid cone, circular conical surface, conulite
One kind (respectively as Figure 14, Figure 15, Figure 16, Figure 17, Figure 18, Figure 19 and Figure 20).
Further, when diversion member 17 is solid cone, hollow centrum or circular conical surface, its basal diameter is less than micro-
The diameter of the open lower side 7 of reaction channel 6 and the greater in the diameter of upper side opening 4, it is preferable that its basal diameter is micro- anti-
4th/to five/10ths of the diameter of the open lower side 7 of passage 6 and the diameter sum of upper side opening 4 are answered, length is not more than
0.9 times of micro- length of reaction channel 6, further, length are 0.1-0.5 times of micro- length of reaction channel 6；When diversion member 17
For hemisphere, hemisphere face, sphere or spheroid when, its spherical diameter be less than micro- reaction channel 6 open lower side 7 diameter and upside
The greater in the diameter of opening 4, it is preferable that its spherical diameter is opened for the diameter of the open lower side 7 of micro- reaction channel 6 with upside
4th/to five/10ths of the diameter sum of mouth 4.The distance between two neighboring diversion member 17 is not less than the water conservancy diversion
The height of element 17.
According to the present invention, diversion member 17 and fixing axle 16 can use metal material, ceramic material, it is preferred to use not with
The metal material that gas in reaction system reacts；The quantity of diversion member 17 can root included by each guiding subassembly 5
Adjusted according to the size and real reaction situation of micro- reaction channel 6, such as can be 3-100.
According to the present invention, in order that reactor can be used in catalytic reaction, the inner surface and/or water conservancy diversion of micro- reaction channel 6
The outer surface of element 17 can be loaded with catalytic active component.Catalytic active component can use well known to those skilled in the art
Catalytic active component, such as when applying to synthesis gas methanation reaction, the active component of load can be anti-with methanation
The metals such as nickel, ruthenium and rhodium that should be active；Described load refer to can by dipping, ion sputtering, coating or filling the methods of
By the catalyst containing active component or directly active component is loaded in micro- reaction channel.Wherein, active metal component applies
The pretreatment and catalyst deposit well-known to those skilled in the art including metallic matrix two can be used by covering loading process
The painting method in stage.
According to the present invention, micro- reaction channel 6 can be in conical pipe, flaring pipe, Y tube and laddertron wherein
A kind of (respectively as shown in Figure 10, Figure 11, Figure 12 and Figure 13).The conical pipe, flaring pipe, Y tube and laddertron can be adopted
With metal material pipe, ceramic material pipe, it is preferred to use the metal tube not reacted with the gas in reaction system.Need to illustrate
, the conventional use of conical pipe of those skilled in the art refers to the truncated cone-shaped hollow material of both ends open, rather than axial cross section
For the section bar of taper.
According to the present invention, in order to ensure the efficiency of chemical reaction, the diameter of micro- reaction channel 6 can 2-50 millimeters it
Between.When applying to the reaction of cumulative volume diminution in course of reaction, the diameter of micro- reaction channel 6 can be from micro- reaction channel 6
Upper side opening 4 is gradually reduced that (diameter of side opening 4 is more than the diameter of open lower side 7 i.e. in guarantee to the direction of open lower side 7
Can, constant situation after also first reducing including channel diameter).It is micro- when applying to the reaction of cumulative volume increase in course of reaction
The diameter of reaction channel 6 can gradually increase from the upper side opening 4 of micro- reaction channel 6 to the direction of open lower side 7 (ensures upside
The diameter of opening 4 is less than the diameter of open lower side 7, also includes the situation of channel diameter increase after first constant).It is described micro- anti-
It can be (0.04-25) to answer the ratio of the diameter of the upper side opening 4 of passage 6 and the diameter of open lower side 7：1, it is preferably (0.1-
10)：1.
According to the present invention, in order to take into account the temperature control of reaction efficiency and reactor, the multiple micro- reaction channel 6 it is interior
The cumulative volume in portion space can all cylinders 12 cumulative volume 30%-90%, preferably 40%-75%.
According to the present invention, the bottoms of the 1# pipes 9 can be provided with it is at least one be used to be distributed be sent into the reactor
The gas distributor of reaction gas.The gas distributor can be conventional use of using those skilled in the art institute, and the present invention is not
Repeat again, the 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, the cylinder 12 of bottom and the bottom surface of housing 1 it
Between can be provided with heat-barrier material area 10.List well-known to those skilled in the art can be placed with the heat-barrier material area 10
The heat-barrier materials such as the heat insulating ball of one material or a variety of composites, heat-insulated felt rug or heat insulating belt.
The present invention is further illustrated by embodiment below in conjunction with accompanying drawing, but therefore the present invention is not taken office
What is limited.
Embodiment 1
As shown in Figure 1 and Figure 5, reactor is provided with 1# pipes 9 including upper end used by the present embodiment, lower end is provided with 2# pipes 11
Pressure-bearing shell 1, the bottom of 1# pipes 9 is provided with first gas distributor 2, and the lower section of first gas distributor 2 is provided with the second gas
Body distributor 14, the lower section of 1# pipes 9, the top of 2# pipes 11 have catalytic reaction zone.What catalytic reaction zone was set from top to bottom including 5
Cylinder 12, space 8, cylinder 12 and the housing 1 of bottom are formed between the cylinder 12 and bottom surface of cylinder 12 and housing 1
The heat-barrier material area 10 being made up of heat-insulated felt rug is provided between bottom surface.Cylinder 12 by upper sealing panel 3 and lower sealing plate 13 and
The internal partial wall of housing 1 is formed, and is to be tightly connected between each other, is hollow in cylinder 12, is provided with each cylinder
2420 (clear to show, to be not entirely shown) axially arranged micro- reaction channel 6.Micro- both ends of reaction channel 6 respectively with cylinder
Top sealing plate 3, cylinder sealed bottom plate 13 are tightly connected；Guiding subassembly 5, diversion member 17 are provided with micro- reaction channel 6
Selection is size identical hemisphere, as shown in figure 14.Micro- reaction channel 6 is as shown in Figure 10 used by the present embodiment
Conical pipe.
The reactor of the present embodiment is provided with 1 pair in the housing sidewall (namely side wall of cylinder) of each side of cylinder 12
Heat transferring medium entrance and heat transferring medium outlet, each pair heat transferring medium entrance and heat transferring medium outlet pass through cylinder chamber fluid respectively
Connection.Heat transferring medium is 196 DEG C of boiler feedwater (13.4MPaG).
A diameter of 550mm of housing 1, highly it is 1500mm.The height of cylinder 12 is 150mm, and used conical pipe is micro-
Reaction channel length is 150mm, conical pipe inlet diameter 10mm, outlet diameter 4mm.Diversion member hemisphere basal diameter is
2.5mm, adjacent guide element spacing are 5mm, and each guiding subassembly includes 15 diversion members (for the ease of sight in embodiment
Examine, do not provide all), diversion member is fixed in reaction channel by fixing axle.The cumulative volume of all micro- reaction channels is post
Body cumulative volume 41.6%.
Reactor proposed by the present invention is applied to synthesis gas methanation reaction, taper pipe internal surface, hemisphere external surface
Supported active metals Ni amounts are 15.2g/m2.Synthesis gas enters reactor from 1# pipes 9, enters successively after two-stage gas distributor
Enter 5 cylinders, methanation reaction occurs in cylinder, reactor is left from reactor bottom by 2# pipes 11.
What is provided in table 1 is the reactor and the contrast situation of axial flow reactor in the prior art that the present embodiment uses.Two kinds
Reactor catalysis reaction zone has identical size, from CO conversion ratios, service life, bed pressure drop, bed temperature and activity gold
Category Ni five indexs of dosage can be seen that reactor proposed by the present invention and all show more excellent performance, especially
Pressure drop, bed temperature and active metal usage amount advantage are fairly obvious.
The reactor of the present embodiment of table 1 contrasts with conventional axial reactor
Embodiment 2
As shown in Figure 2 and Figure 5, the housing inner diameter, cylinder, microchannel of the present embodiment reactor and the reactor of embodiment 1
It is identical Deng structural parameters.Difference from Example 1 is that what diversion member 17 selected in the present embodiment is size identical ball
Body, as shown in figure 17.
The present embodiment can be equally used for synthesis gas methanation reaction, under identical process conditions, CO conversion ratios, CH4
Selectivity, service life are identical with the data obtained using reactor in embodiment 1, and difference is, in the present embodiment
Bed temperature for 581 DEG C, pressure drop 2.8kPa, active metal Ni usage amounts be 1.35kg.
Embodiment 3
As shown in Figure 3 and Figure 6, the reactor shell internal diameter of the present embodiment reactor and embodiment 1, cylinder, microchannel, lead
The structural parameters such as fluid element are identical.Difference is that the reactor of the present embodiment goes out heat transferring medium entrance and heat transferring medium
Mouth is arranged on the side in space 8, and heat transferring medium entrance passes through 5 groups of heat exchanger assemblies 15 and corresponding heat transferring medium outlet.
As shown in fig. 6, heat exchanger assembly 15 is plate-like coiling pipeline, heat transferring medium entrance is communicated in plate-like coiling pipeline first
The heart, then from inside to outside finally with heat transferring medium outlet.Heat transferring medium is 145 DEG C of boiler feedwater (13.5MPaG).
The reactor that the present embodiment uses can be applied to synthesis gas and synthesize C in Fe bases catalyst2 =、C3 =Deng small-numerator olefin.
Taper pipe internal surface, hemisphere external surface supported active metals Fe amounts are 17.5g/m2.Synthesis gas enters reactor from 1# pipes, from
The 2# pipes discharge reactor of reactor bottom.
What is provided in table 2 is the reactor and the contrast situation of axial flow reactor in the prior art that the present embodiment uses.Two kinds
Reactor catalysis reaction zone has identical size, from CO conversion ratios, service life, bed pressure drop, bed temperature and activity gold
Category Fe five indexs of dosage can be seen that reactor proposed by the present invention and all show more excellent performance.
The reactor of the present embodiment of table 2 contrasts with conventional axial reactor
Embodiment 4
The reactor shell internal diameter that as shown in Figure 4 and Figure 6, is used used by the present embodiment in reactor and embodiment 2,
The structural parameters such as cylinder, micro- reaction channel, diversion member are identical.Difference from Example 2 is, the reactor of the present embodiment
Heat transferring medium entrance and heat transferring medium outlet are arranged on to the side in space 8, heat transferring medium entrance passes through 5 groups of heat exchanger assemblies 15
With corresponding heat transferring medium outlet.As shown in fig. 6, heat exchanger assembly 15 is plate-like coiling pipeline, heat transferring medium entrance is first
First be communicated to the center of plate-like coiling pipeline, then from inside to outside finally with heat transferring medium outlet.Heat transferring medium is 145 DEG C
Boiler feedwater (13.5MPaG).
The present embodiment can be equally used for preparation of low carbon olefines by synthetic gas reaction, under identical process conditions, service life
It is identical with the data obtained using reactor in embodiment 3.Difference is that CO conversion ratios are 39.5%, bed temperature
It is 1.85kg for 285 DEG C, pressure drop 3.15kPa, active metal Fe usage amounts.
Embodiment 5
Reactor and the reactor shell internal diameter, cylinder, micro- reaction that are used in embodiment 4 are logical used by the present embodiment
The structural parameters such as road, diversion member are identical.Difference is that cylinder is inverted by the present embodiment, i.e., micro- reaction is logical in the present embodiment
The upper side opening in road is diameter small end, open lower side is to be relatively large in diameter end.
Because micro- reaction channel inlet diameter gradually increases to outlet diameter, the reactor can be used for urging for volume increase
Change reaction, such as microchannel inner surface, diversion member outer surface of spheroid load Fe2O3Active component, heat transferring medium 40wt%
NaNO2, 7wt%NaNO3, 53wt%KNO3, when the temperature of heat transferring medium is 560 DEG C, can be used for ethyl benzene dehydrogenation preparation of styrene.
Pressure drop drops to 1.3kPa from the 5.4kPa of conventional axial reactor, and Fe2O3Usage amount have decreased to 2.25kg from 50.5kg.
Conversion of ethylbenzene rises to 72% from 60%.It can be seen that the catalytic reactor used in the present embodiment shows excellent performance.
Catalytic reactor provided by the invention is compact-sized, active metal dosage is few, bed pressure drop is small, the product residence time
Short, feed stock conversion 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 to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
- A kind of 1. isothermal reactor, it is characterised in that：The reactor includes radial direction cylindrical shape seal and pressure bearing housing (1), from described The 1# pipes (9) of enclosure interior are extend at the top of housing (1), extend into from the housing (1) bottom enclosure interior 2# pipes (11), The catalytic reaction zone that is arranged in the housing (1) below 1# pipe (9) above the 2# pipes (11) and for it is described The heat transmission equipment of catalytic reaction zone heat exchange；The catalytic reaction zone includes at least one cylinder (12), the cylinder (12) with the housing (1) coaxially, and the post The medial surface of the lateral surface of body (12) and the housing (1) is inconsistent or coincides；Between two neighboring cylinder (12), bottom Cylinder (12) and housing (1) bottom surface between formed with space (8)；Multiple axial directions are provided with each described cylinder (12) It is between the 1# pipes (9) and uppermost space (8) and two neighboring through micro- reaction channel (6) of the cylinder (12) Only it is in fluid communication between space (8) by micro- reaction channel (6), space (8) and the 2# pipes (11) of bottom are in fluid communication；The guiding subassembly (5) of increase Hydrodynamic turbulence effect is provided with micro- reaction channel (6).
- 2. reactor according to claim 1, wherein, by each inwall of the cylinder (12) and each in each described cylinder (12) The outer wall of micro- reaction channel (6) has been collectively forming a cylinder chamber；The heat transmission equipment is included in corresponding to each cylinder (12) at least one pair of heat transferring medium entrance being located remotely from each other and the heat transferring medium outlet set on the housing (1) of side, The heat transferring medium entrance passes through the cylinder chamber and the heat transferring medium communication.
- 3. reactor according to claim 1, wherein, the heat transmission equipment is included in corresponding to space each described (8) At least one pair of heat transferring medium entrance being located remotely from each other for being set on the housing (1) of side, heat transferring medium outlet and through sky The heat exchanger assembly of gap (8), the heat transferring medium entrance are flowed by the heat exchanger assembly (15) and heat transferring medium outlet Body connects, and the heat exchanger assembly (15) is selected from tubular coiling pipeline, ring-type coiling pipeline, plate-like coiling pipeline and heat exchanger plates At least one of.
- 4. reactor according to claim 1, wherein, the quantity of the cylinder (12) is 2-500.
- 5. reactor according to claim 1, wherein, the guiding subassembly (5) includes and the fixed company of micro- reaction channel (6) The fixing axle (16) connect and the diversion member (17) being connected in the fixing axle (16), the diversion member (17) is described in One end of micro- reaction channel (6) airintake direction is convex.
- 6. reactor according to claim 5, wherein, the diversion member (17) is selected from solid cone, hollow centrum, circle At least one of the conical surface, hemisphere, hemisphere face, spheroid and sphere.
- 7. reactor according to claim 6, wherein, the basal diameter of the solid cone, hollow centrum and circular conical surface is small The diameter of open lower side (7) in micro- reaction channel (6) and the greater in the diameter of upper side opening (4)；The hemisphere, half The spherical diameter of sphere, sphere and spheroid is less than the diameter and upper side opening (4) of the open lower side (7) of micro- reaction channel (6) The greater in diameter；The spacing of the two neighboring diversion member (17) is not less than the height of the diversion member (17).
- 8. reactor according to claim 5, wherein, each guiding subassembly (5) includes the 3-100 diversion members (17)。
- 9. reactor according to claim 5, wherein, the inner surface of micro- reaction channel (6) and/or diversion member (17) Outer surface is loaded with catalytic active component.
- 10. reactor according to claim 1, wherein, micro- reaction channel (6) is selected from conical pipe, flaring pipe, Y shape One of which in pipe and laddertron；The diameter of micro- reaction channel (6) is between 2-50 millimeters；The upper side opening (4) The ratio of diameter of diameter and open lower side (7) be (0.04-25)：1；The inner space of micro- reaction channel (6) it is total Volume is the 30%-90% of the cumulative volume of all cylinders (12).
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| CN201610342292.6A CN107398238A (en) | 2016-05-20 | 2016-05-20 | A kind of isothermal reactor |
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| CN201610342292.6A CN107398238A (en) | 2016-05-20 | 2016-05-20 | A kind of isothermal reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109395670A (en) * | 2018-09-30 | 2019-03-01 | 中石化宁波工程有限公司 | The temperature shift reactions device such as alternating temperature |
| CN113209922A (en) * | 2020-01-21 | 2021-08-06 | 中国石油化工股份有限公司 | Microwave coupling catalytic reactor and VOCs treatment facility |
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| CN103301799A (en) * | 2013-04-18 | 2013-09-18 | 万华化学集团股份有限公司 | Reactor for preparing isophorone nitrile and method for continuously preparing isophorone nitrile by adopting reactor |
| CN203540504U (en) * | 2013-09-23 | 2014-04-16 | 中国五环工程有限公司 | Isothermal micro-reaction methanation system |
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| CN103301799A (en) * | 2013-04-18 | 2013-09-18 | 万华化学集团股份有限公司 | Reactor for preparing isophorone nitrile and method for continuously preparing isophorone nitrile by adopting reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109395670A (en) * | 2018-09-30 | 2019-03-01 | 中石化宁波工程有限公司 | The temperature shift reactions device such as alternating temperature |
| CN109395670B (en) * | 2018-09-30 | 2022-04-12 | 中石化宁波工程有限公司 | Temperature-changing isothermal transformation reaction device |
| CN113209922A (en) * | 2020-01-21 | 2021-08-06 | 中国石油化工股份有限公司 | Microwave coupling catalytic reactor and VOCs treatment facility |
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