CN106861590A - Aromatic hydrocarbons conversion reactor - Google Patents
Aromatic hydrocarbons conversion reactor Download PDFInfo
- Publication number
- CN106861590A CN106861590A CN201710091559.3A CN201710091559A CN106861590A CN 106861590 A CN106861590 A CN 106861590A CN 201710091559 A CN201710091559 A CN 201710091559A CN 106861590 A CN106861590 A CN 106861590A
- Authority
- CN
- China
- Prior art keywords
- ring
- housing
- heat
- aromatic hydrocarbons
- pipe
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- B01J19/24—Stationary reactors without moving elements inside
-
- 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
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- 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
- B01J19/0053—Details of the reactor
-
- 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
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
-
- 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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/004—Sparger-type elements
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/39—Preparation of carboxylic acid esters by oxidation of groups which are precursors for the acid moiety of the ester
-
- 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
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
-
- 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
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/185—Details relating to the spatial orientation of the reactor vertical
-
- 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
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/322—Basic shape of the elements
- B01J2219/32203—Sheets
Abstract
The invention provides a kind of aromatic hydrocarbons conversion reactor, including housing, enclosure interior is sequentially provided with gas distributor, at least one set of heat-exchanger rig, broken bubble component and gas-liquid separator from the bottom to top, multiple air admission holes are offered in housing sidewall, air admission hole connection gas distributor inside and hull outside, heat exchange entrance is further opened with housing sidewall and heat exchange is exported, heat exchange entrance and heat exchange outlet are connected with heat-exchanger rig respectively, and case top offers steam vent, steam vent is connected with gas-liquid separator, and housing bottom offers the product exit that can be opened and closed.The aromatic hydrocarbons conversion reactor that the present invention is provided, can be uniform to enclosure interior bubbling in housing bottom；Air pocket can be broken into by minute bubbles, increase gas and the contact area of reactant when multiple bubbles pool air pocket by broken bubble component simultaneously, reaction efficiency is improved；Reaction heat is efficiently removed by heat-exchanger rig, and by the moisture content of gas-liquid separator reduction gas-phase product, reduces downstream dehydration pressure.
Description
Technical field
The present invention relates to aromatic hydrocarbons transformation technology field, a kind of aromatic hydrocarbons conversion reactor is referred in particular to.
Background technology
Dimethylbenzene liquid phase oxidation is that under catalyst action, aromatic hydrocarbons reacts rapidly after being oxidized to acid with alcohol in aromatic hydrocarbons conversion
Generation ester, while the process of big calorimetric is released, wherein needing oxygen (or air) participation.Therefore uniform gas distribution, height
The heat exchange of effect, the lifting of reaction efficiency, outlet gas-liquid separation will be used as structure of reactor developing focus.Existing aromatic hydrocarbons conversion is anti-
It is that gas passes through liquid (slurries) layer in bubbling form to answer device, to realize the reactor of course of reaction.Current most domestic gas
Body distributor mainly enters the heat exchange structure commonly used in bed, and reactor by single entrance through circle distributor C-shaped ring
Pipe, coiled pipe and spiral coil etc..
Wherein, prior art aromatic hydrocarbons conversion reactor have that bubbling is uneven mostly, bubbling it is larger cause reaction efficiency compared with
The shortcomings of low and uneven heat exchange.
The content of the invention
It is uniform it is an object of the invention to provide a kind of bubbling, and the smaller aromatic hydrocarbons so as to effectively improve reaction efficiency of bubbling turn
Change reactor.
To reach above-mentioned purpose, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, the aromatic hydrocarbons conversion reactor
Including housing, the inside of the housing be sequentially provided with from the bottom to top gas distributor, at least one set of heat-exchanger rig, broken bubble component and
Gas-liquid separator, offers multiple air admission holes on the side wall of the housing, the air admission hole connects the interior of the gas distributor
The outside of portion and the housing, is further opened with heat exchange entrance on the side wall of the housing and heat exchange is exported, the heat exchange entrance with
The heat exchange outlet connect with the heat-exchanger rig respectively, and steam vent is offered at the top of the housing, the steam vent and
The gas-liquid separator connection, the bottom of the housing offers the product exit that can be opened and closed；
The gas distributor includes many air inlet supervisors, and each air inlet supervisor sets along radially extending for the housing
Put, each air inlet supervisor includes a blind end and an open end, and the open end is passed through in multiple air admission holes
An outside for extending out to the housing, and the blind end extends to the center of the radial section of the housing, each institute
The lower section connection for stating air inlet supervisor is provided with multiple vertical branch pipes for extending axially downward along the housing, each described air inlet master
Many vertical branch pipes below pipe along the housing radial arrangement, the lower end of each vertical branch pipe connects and sets
There is an arc branch pipe, and the lower surface of each arc branch pipe offers multiple spray orifices.
Aromatic hydrocarbons conversion reactor as described above, wherein, the broken bubble component includes support frame and multiple broken bubble rings, described
Support frame is fixed on the inwall of the housing, and support frame as described above is located at the top of the gas distributor, multiple described broken
Bubble ring is uniformly distributed on support frame as described above.
Aromatic hydrocarbons conversion reactor as described above, wherein, the broken bubble ring includes ring frame and outside the annular
The disk in inframe portion, the disk is arranged concentrically with the ring frame, by many between the disk and the ring frame
Individual broken bubble piece connection, each broken bubble piece is uniformly distributed along the setting that radially extends of the disk, and multiple broken bubble pieces
Between the disk and the ring frame, and it is uniformly distributed on the disk and is provided with through hole.
Aromatic hydrocarbons conversion reactor as described above, wherein, support frame as described above includes the first ring, the second ring and multiple gussets,
First ring is fixed on the inwall of the housing by the gusset, and second ring is located at the inside of first ring,
It is uniformly distributed between first ring and the inwall of the housing and is provided with multiple broken bubble rings, and first ring and described the
It is uniformly distributed between two rings and is provided with multiple broken bubble rings, each broken bubble ring is by the gusset and first ring, described the
The inwall connection of two rings and/or the housing, multiple positioning pipes, institute are connected with first ring and second ring respectively
Positioned in stating the lower end of heat-exchanger rig and inserting multiple positioning pipes.
Aromatic hydrocarbons conversion reactor as described above, wherein, the heat-exchanger rig includes multigroup heat-exchanging tube bundle and set pipe fitting,
The set pipe fitting includes cooling water concetrated pipe, steam set pipe and two plugging sheets, and two plugging sheets close off institute
The two ends of steam set pipe are stated, the cooling water concetrated pipe is located at the inside of the steam set pipe, and the steam set pipe
It is coaxially disposed with the cooling water concetrated pipe, the two ends of the cooling water concetrated pipe are tightly connected with plugging sheet described in two respectively,
The first closed ring cavity, the inside of the cooling water concetrated pipe are formed between the cooling water concetrated pipe and the steam set pipe
Connected with the heat exchange entrance by pipeline, first ring cavity passes through pipeline and the heat exchange outlet, the heat exchanger tube
Beam is connected with the inside of first ring cavity and the cooling water concetrated pipe.
Aromatic hydrocarbons conversion reactor as described above, wherein, the heat-exchanging tube bundle includes inner tube and is sheathed on said inner tube
The outer tube in outside, said inner tube is set with the outer coaxial tube, and the second ring cavity is formed between said inner tube and the outer tube, described
The upper end of inner tube sequentially through the steam set pipe and the cooling water concetrated pipe and with the inside of the cooling water concetrated pipe
Connection, the lower end of said inner tube extends downward at the lower end of the outer tube and is connected with second ring cavity, the outer tube
Lower end is sealed by end socket, during the upper end of the outer tube stretches to first ring cavity through the steam set pipe, described the
One ring cavity is connected with second ring cavity.
Aromatic hydrocarbons conversion reactor as described above, wherein, the heat-exchanging tube bundle also includes many evaporation tubes, many steamings
Outer tube described in hair Guan Junyu is parallel, and many evaporation tubes are uniformly distributed in around the outer tube, the every evaporation tube
Upper end connected with second ring cavity through the upper end side wall of the outer tube, and the lower end of the every evaporation tube is run through
The bottom side of the wall of the outer tube is connected with second ring cavity.
Aromatic hydrocarbons conversion reactor as described above, wherein, the gas-liquid separator includes inner cylinder, the upper end of the inner cylinder with
The top inner wall of the housing is tightly connected, and the lower end of the inner cylinder is provided with base plate in which can be removably mounted, and the base plate closing is described
The lower end of inner cylinder, the inside of the inner cylinder passes through the ft connection of the steam vent and the housing, on the side wall of the inner cylinder
Offer and be covered with silk screen in multiple perforation, and each perforation.
Aromatic hydrocarbons conversion reactor as described above, wherein, the gas-liquid separator also includes outer barrel, and the outer barrel is set in
The outside of the inner cylinder, and the inner cylinder is coaxially disposed with the outer barrel, and the 3rd ring is formed between the inner cylinder and the outer barrel
Chamber, the upper end of the outer barrel is connected with the top inner wall of the housing, and the inwall of the outer barrel is provided with multiple first baffles, edge
The direction towards the axis near the inner cylinder, each first baffle is inclined by up to lower, on the outer wall of the inner cylinder
Multiple second baffles are provided with, along the direction of the axis for being directed away from the inner cylinder, each second baffle is by up to having a down dip
Tiltedly.
Aromatic hydrocarbons conversion reactor as described above, wherein, connected by many lacing wires between the inner cylinder and the outer barrel.
Compared with prior art, advantages of the present invention is as follows：
The aromatic hydrocarbons conversion reactor that the present invention is provided, gas distributor is responsible for by many air inlets, vertical branch pipe and arc
The setting of shape branch pipe, equally distributed many spray orifices are formed with the bottom of housing, can the bottom even of housing to
Enclosure interior bubbling；Simultaneously by set broken bubble component air pocket can be broken into when multiple bubbles pool air pocket it is stingy
Bubble, so that increase the contact area of gas and reactant, so as to improve reaction efficiency.
Brief description of the drawings
The following drawings is only intended to, in schematic illustration and explanation is done to the present invention, not delimit the scope of the invention.Wherein：
Fig. 1 is the structural representation of the aromatic hydrocarbons conversion reactor that the present invention is provided；
Fig. 2 is the structural representation of the heat-exchanger rig of the aromatic hydrocarbons conversion reactor that the present invention is provided；
Fig. 3 is the cross-sectional view of the A-A hatchings along Fig. 2；
Fig. 4 is the structural representation of the heat-exchanging tube bundle of the heat-exchanger rig of the aromatic hydrocarbons conversion reactor that the present invention is provided；
Fig. 5 is the gas distributor of the aromatic hydrocarbons conversion reactor that the present invention is provided along the generalized section of housing axial direction；
Fig. 6 is the generalized section of the B-B hatchings along Fig. 5；
Fig. 7 is the generalized section of the C-C hatchings along Fig. 6；
Fig. 8 is the structural representation of the broken bubble component of the aromatic hydrocarbons conversion reactor that the present invention is provided；
Fig. 9 is the structural representation of the broken bubble ring of the broken bubble component of the aromatic hydrocarbons conversion reactor that the present invention is provided；
Figure 10 is the structural representation of the gas-liquid separator of the aromatic hydrocarbons conversion reactor that the present invention is provided.
Drawing reference numeral explanation：
1 housing
2 gas distributors
21 air inlets are responsible for
22 vertical branch pipes
23 arc branch pipes
231 spray orifices
3 heat-exchanger rigs
31 heat-exchanging tube bundles
311 inner tubes
312 outer tubes
313 second ring cavities
314 evaporation tubes
32 set pipe fittings
321 cooling water concetrated pipes
322 steam set pipes
323 first ring cavities
33 plugs
34 end sockets
4 broken bubble components
41 support frames
411 first rings
412 second rings
413 gussets
414 positioning pipes
42 broken bubble rings
421 ring frames
422 disks
423 broken bubble pieces
5 gas-liquid separators
51 inner cylinders
511 base plates
512 silk screens
513 second baffles
52 outer barrels
521 first baffles
53 lacing wires
54 the 3rd ring cavities
Specific embodiment
In order to have clearer understanding to technical scheme, purpose and effect, in conjunction with the brief description of the drawings present invention
Specific embodiment.
As shown in figure 1, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, aromatic hydrocarbons conversion reactor includes (closed
) housing 1, the inside of housing 1 is sequentially provided with gas distributor 2, at least one set of heat-exchanger rig 3, broken bubble component 4 and from the bottom to top
Gas-liquid separator 5, broken bubble component 4 is for the larger bubble in the inside of housing 1 to be broken into minute bubbles, to increase gas with reaction
The contact area of thing, improves reaction efficiency.When heat-exchanger rig 3 is set to multigroup, multigroup heat-exchanger rig 3 is to be spaced up and down
Setting (is provided with two groups of heat-exchanger rigs 3, those skilled in the art can according to actual needs choose heat-exchanger rig 3 in Fig. 1
Group number, the present invention is not limited thereto), multiple air admission holes are offered (at the lower end of housing 1) on the side wall of housing 1, enter
The inside of stomata connection gas distributor 2 is with the outside of housing 1, the i.e. inside of gas distributor 2 by air admission hole and housing 1
Ft connection, the gas outside housing 1 enters to the inside of gas distributor 2 by air admission hole, and equal by gas distributor 2
The even inside for blasting housing 1, for aromatic hydrocarbons conversion reaction provides oxygen, is further opened with being connected with heat-exchanger rig 3 on the side wall of housing 1
Heat exchange entrance and heat exchange export, heat transferring medium is produced into absorbing aromatic hydrocarbons conversion reaction in heat-exchanger rig 3 by the entrance that exchanges heat
Heat, then from heat exchange outlet discharge, by aromatic hydrocarbons conversion reaction produce waste heat take away, to ensure the temperature in housing 1
Degree is within the scope of the temperature required for aromatic hydrocarbons conversion reaction, and the top of housing 1 offers steam vent, steam vent and gas-liquid point
Connected from device 5, the gas phase produced after aromatic hydrocarbons conversion reaction can carry some tiny drops secretly in upward motion process, by gas
The drop mixed with gas phase can be separated and stay in the inside of housing 1 by liquid/gas separator 5 from gas phase, and gas phase is then
The outside of housing 1 can be expelled to through steam vent, the bottom of housing 1 offers the product exit that can be opened and closed, aromatic hydrocarbons conversion reaction
The liquid product of generation is expelled to the outside of housing 1 from product exit；
As shown in Fig. 5~Fig. 7, gas distributor 2 includes many air inlet supervisors 21, and each air inlet supervisor 21 is along housing 1
Setting is radially extended, one end of each air inlet supervisor 21 passes through an outside for extending out to housing 1 in multiple air admission holes, housing 1
Outside gas enters to the inside that air inlet is responsible for 21, air inlet master by one end stretched to outside housing 1 that air inlet is responsible for 21
Welded between the outer wall and air admission hole of pipe 21, prevent the reactant inside housing 1 from being leaked by air admission hole, and each air inlet supervisor 21
The other end extend to housing 1 radial section center, i.e. each air inlet supervisor 21 includes a closing for end-enclosed
End and an open end for end insertion, open end pass through an outside for extending out to housing 1 in multiple air admission holes, and closing
End extends to the center of the radial section of housing 1；On the radial section of housing 1, each two it is adjacent air inlet supervisor 21 it
Between the angle that is formed it is identical, i.e., multiple air inlets supervisors 21 are evenly distributed on one of radial section of housing 1；Each air inlet master
The lower section connection of pipe 21 is provided with multiple vertical branch pipes 22 for extending axially downward along housing 1, the gas in each air inlet supervisor 21
Body cannot be discharged from blind end, can only be even into coupled logical multiple vertically branch pipes 22 in, under each air inlet supervisor 21
Side many vertical branch pipes 22 along housing 1 radial arrangement, the lower end of each vertical branch pipe 22 connects and is provided with an arc
Branch pipe 23 so that the arc branch pipe 23 of each lower end of vertical branch pipe 22 is communicated in multiple air inlets along the radial arrangement of housing 1
The arc branch pipe 23 of the vertical lower end of branch pipe 22 of multiple of supervisor 21 is enclosed in the inside of housing 1 and forms multiple concentric circles, and respectively
The lower surface of arc branch pipe 23 uniformly offers multiple spray orifices 231, and corresponding arc branch pipe 23 is entered by vertical branch pipe 22
In gas be uniformly distributed and along the bottom of arc branch pipe 23 multiple spray orifices 231 uniformly spray, i.e., gas to be formed along enclosing
The inside jet to housing 1 of the bottom even of the arc branch pipe 23 of multiple concentric circles so that bed bubbling is uniform, so as to ensure
Aromatic hydrocarbons conversion reaction is uniformly carried out.The distribution mode of wherein spray orifice 231 is not limited only to shown in figure, and spray orifice 231 is a diameter of
2mm~20mm, for the positions and dimensions of spray orifice 231, those skilled in the art can be according to specific aromatic hydrocarbons conversion reaction spirit
Living to select, the present invention is not limited thereto.
Preferably, as shown in fig. 6, in the aromatic hydrocarbons conversion reactor of present invention offer, air inlet supervisor 21 is provided with four, often
Angle between two adjacent air inlet supervisors 21 is 90 °, and gas distributor 2 is divided into four areas as can be seen from Figure 6,
Ensure that basic air inflow.It should be noted that air inlet can be responsible for 21 by those skilled in the art according to actual needs
Radical be set to other numbers, the present invention is not limited thereto.
The aromatic hydrocarbons conversion reactor that the present invention is provided, can effectively solve each nozzle tolerance of distributor of existing reactor not
, bed bubbling is uneven, react on uneven, bed cross section that temperature distributing disproportionation is even, be unfavorable for the removal of reaction heat, big
Bubbling is more and bed reaction mass contact area is small, reaction efficiency is relatively low, heat exchange structure manufacture is complicated, be unfavorable for reactor
Amplify, must be exchanged heat using forced circulation, will thoroughly lose the kinetic energy of heat exchange under limit power failure operating mode, easily cause temperature runaway and
The gaseous phase outlet band technical problem such as liquid measure is big, with bubbling it is more uniform, reaction efficiency is higher, heat transfer effect is more preferable, bed temperature
Degree gradient is small, heat exchange structure is simple to manufacture, it is easy to the advantages of amplifying and greatly reduce gaseous phase outlet band liquid measure.
Further, as shown in figure 8, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, broken bubble component 4 includes
Support frame 41 and multiple broken bubble rings 42, support frame 41 is fixed on the inwall of housing 1, and support frame 41 is located at gas distributor 2
Top, multiple broken bubble rings 42 are uniformly distributed on support frame 41.From the bubble in the penetrating liquid of gas distributor 2 from the bottom to top
Motion, when reaching broken bubble ring 42, for the bubble of some large-sizes, broken bubble ring 42 is crushed, and is turned into it multiple small
Bubble, so as to increase the contact area of bubble and reactant, improves reaction efficiency.
Further, as can be seen from figures 8 and 9, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, broken bubble ring
42 include ring frame 421 and the disk 422 inside ring frame 421, and disk 422 is arranged concentrically with ring frame 421,
Connected by multiple broken bubble pieces 423 between disk 422 and ring frame 421, each broken bubble piece 423 prolongs along the radial direction of disk 422
Setting is stretched, and multiple broken bubble pieces 423 are uniformly distributed between disk 422 and ring frame 421, and be uniformly distributed on disk 422
It is provided with through hole.During present invention operation, risen into the bubble of bed by the gas distributor 2 of the bottom of housing 1
Cheng Zhonghui is constantly collected as larger bubble, and the effect of broken bubble ring 42, is exactly smashed when air pocket is passed through as stingy
Bubble, and then increase the contact area of gas and bed material, improve reaction efficiency.In the upward motion process of bubble of large-size
Can be broken into multiple minute bubbles when touching broken bubble piece 423, minute bubbles from passed through between the adjacent broken bubble piece 423 of each two or from
Through hole on disk 422 is passed through and continued up, wherein to improve crushing effect, can set the edge of broken bubble piece 423
For zigzag, it is necessary to explanation, every for the broken number for steeping ring 42, the distributing position of broken bubble ring 42 and each broken bubble ring 42
Between two adjacent broken bubble pieces 423 supply bubble through size can flexibly be selected according to actually required reaction rate, this hair
It is bright to be not limited thereto.
Further, as shown in figure 8, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, support frame 41 includes the
One ring 411, the second ring 412 and multiple gussets 413, the first ring 411 are fixed on the inwall of housing 1 by gusset 413, the second ring
412 inside for being located at the first ring 411, are uniformly distributed between the first ring 411 and the inwall of housing 1 and are provided with multiple broken bubble rings 42, and
It is uniformly distributed between first ring 411 and the second ring 412 and is provided with multiple broken bubble rings 42, each broken bubble ring 42 is by gusset 413 and the
The inwall connection of one ring 411, the second ring 412 and/or housing 1, it is to be understood that can between the first ring 411 and the second ring 412
Being connected and be indirectly fixed to together by being connected to broken bubble ring 42 positioned there between, or, the He of the first ring 411
Multiple gussets 413 can also be directly set to being directly linked together, the present invention is not limited thereto between second ring 412；It is right
Multiple positioning pipes 414, heat-exchanger rig 3 should be respectively connected with the lower end of heat-exchanger rig 3, the first ring 411 and the second ring 412
Lower end can insert multiple positioning pipes 414 in positioned, to ensure that heat-exchanger rig 3 can keep flat with the axis of housing 1 all the time
OK, constrain heat-exchanger rig 3 horizontal displacement, it is to avoid heat-exchanger rig 3 vibrate and housing 1 inside shaking and collide housing 1
Inwall.
Wherein, please also refer to Fig. 3 and Fig. 8, from Fig. 3 and Fig. 8 as can be seen that in Fig. 3 each heat-exchanging tube bundle 31 it is outer
The position of pipe 312 corresponds respectively to the position of each positioning pipe 414 in Fig. 8, when mounted, by the outer tube of each heat-exchanging tube bundle 31
312 lower end is inserted into corresponding each positioning pipe 414, so that the axis of each heat-exchanging tube bundle 31 is protected with the axis of housing 1
Maintain an equal level row, constrains the horizontal displacement of heat-exchanging tube bundle 31.
Further, as shown in Fig. 2 the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, heat-exchanger rig 3 includes
Multigroup heat-exchanging tube bundle 31 and set pipe fitting 32, set pipe fitting 32 include cooling water concetrated pipe 321, steam set pipe 322 and two
Plugging sheet, two plugging sheets close off the two ends of steam set pipe 322, and cooling water concetrated pipe 321 is located at steam set pipe 322
Inside, and steam set pipe 322 is coaxially disposed with cooling water concetrated pipe 321, and the two ends of cooling water concetrated pipe 321 are respectively with two
Plugging sheet is tightly connected, and the first closed ring cavity 323, i.e., two are formed between cooling water concetrated pipe 321 and steam set pipe 322
Two closed spaces are formd between plugging sheet and cooling water concetrated pipe 321, steam set pipe 322, one of them is to be located at
The first ring cavity 323 between cooling water concetrated pipe 321 and steam set pipe 322, another is the interior of cooling water concetrated pipe 321
Portion, the inside of cooling water concetrated pipe 321 is connected by pipeline with heat exchange entrance, and the first ring cavity 323 is exported by pipeline with heat exchange
Connection, heat-exchanging tube bundle 31 is connected with the inside of the first ring cavity 323 and cooling water concetrated pipe 321.The relatively low heat transferring medium of temperature from
Heat exchange entrance enters in cooling water concetrated pipe 321, and the heat transferring medium in cooling water concetrated pipe 321 respectively enters multigroup heat-exchanging tube bundle
Exchanged heat in 31, temperature heat transferring medium higher enters in the first ring cavity 323 in each group heat-exchanging tube bundle 31 after heat exchange, and leads to
Cross heat exchange outlet to be discharged from the first ring cavity 323, completion once exchanges heat.
Further, as shown in Figures 3 and 4, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, heat exchanger tube
Beam 31 includes inner tube 311 and is sheathed on the outer tube 312 in the outside of inner tube 311, and inner tube 311 is coaxially disposed with outer tube 312, inner tube
The second ring cavity 313 is formed between 311 and outer tube 312, steam set pipe 322 and cooling water collection are sequentially run through in the upper end of inner tube 311
Close pipe 321 and connected with the inside of cooling water concetrated pipe 321, you can be interpreted as, the first ring cavity is run through in the upper end of inner tube 311
The inside of cooling water concetrated pipe 321 is stretched to after 323 and is connected with the inside of cooling water concetrated pipe 321, inner tube 311 is not with first
Ring cavity 323 is connected, and the lower end of inner tube 311 extends downward at the lower end of outer tube 312 and connected with the second ring cavity 313, i.e. inner tube
311 lower end is not connected to the lower end of outer tube 312, between making to have necessarily between the lower end of inner tube 311 and the lower end of outer tube 312
Gap, and the inside of inner tube 311 connected by the gap with the second ring cavity 313, the lower end of outer tube 312 is sealed by end socket 34, outward
(the first ring cavity 323 is stretched into through steam set pipe 322 and with the inside for stretching to steam set pipe 322 in the upper end of pipe 312
In), the first ring cavity 323 is connected with the second ring cavity 313.It is arranged such, the relatively low heat transferring medium of temperature is from cooling water concetrated pipe 321
In middle entrance inner tube 311, and upper end along inner tube 311 moves downwardly to the lower end of inner tube 311, in the inside of inner tube 311, temperature
Relatively low heat transferring medium is tentatively exchanged heat, and is turned back after end socket 34 is arrived at, by under the lower end of inner tube 311 and outer tube 312
Gap between end enters in the second ring cavity 313, gradually increases then as the heat transferring medium for entering, and is changed in the second ring cavity 313
The liquid level of thermal medium gradually rises and enters the first ring cavity 323, and temperature heat transferring medium higher is by exchanging heat out after finally exchanging heat
Mouth is expelled to the outside of the first ring cavity 323, completes whole heat transfer process.
Wherein, it is uniform in the section heat exchange of aromatic hydrocarbons conversion reactor of the present invention to ensure, thermograde is reduced to greatest extent,
Each group heat-exchanging tube bundle 31 is as shown in Figure 7 in the radial section arrangement of aromatic hydrocarbons conversion reactor of the present invention so that uniform point of each tube bank
Cloth is in the inside of housing 1, so as to ensure aromatic hydrocarbons conversion reactor energy uniform heat exchange of the invention.For above-mentioned heat-exchanger rig 3
The arrangement mode of each heat-exchanging tube bundle 31 and the structure type of heat-exchanging tube bundle 31 be present pre-ferred embodiments, it is necessary to illustrate
, the arrangement mode of each heat-exchanging tube bundle 31 can be discharged flexibly according to actual needs in heat-exchanger rig 3, while heat-exchanging tube bundle 31
There can also be other structures, as long as can play a part of the present invention effectively improves heat exchange efficiency, the present invention is not with this
It is limited.
Preferably, as shown in Figure 2 to 4, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, heat-exchanging tube bundle
31 also include many evaporation tubes 314, and many evaporation tubes 314 are parallel with outer tube 312, and many evaporation tubes 314 are uniformly distributed in
Around outer tube 312, the every upper end of evaporation tube 314 connects through the upper end side wall of outer tube 312 with the second ring cavity 313, and
The every lower end of evaporation tube 314 connects through the bottom side of the wall of outer tube 312 with the second ring cavity 313.Enter in heat transferring medium
While two ring cavity 313, according to the principle of linker, heat transferring medium enters each evaporation connected with the second ring cavity 313 simultaneously
In pipe 314, and liquid level in each evaporation tube 314 remains concordant with the liquid level in the second ring cavity 313, in the second ring cavity
While heat transferring medium in 313 is exchanged heat with reactant, the heat transferring medium of evaporation tube 314 is also exchanged heat with reactant,
Therefore, can effectively increase the heat exchange area of heat transferring medium and reactant by setting evaporation tube 314, effectively improve heat exchange efficiency.
Preferably, as shown in figure 4, the present invention provide aromatic hydrocarbons conversion reactor in, because heat-exchanging tube bundle 31 is vertical
Place, during present invention operation, the impurity in heat transferring medium is easily piled up in end socket 34 and causes subtracting for meteorological spatial
It is few, therefore, the present invention sets plug 33 in the bottom of outer tube 312, convenient that it is overhauled and is cleared up.
Further, as shown in Figure 10, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, gas-liquid separator 5 is wrapped
Inner cylinder 51 is included, upper end and the top inner wall of housing 1 of inner cylinder 51 are tightly connected, and the lower end of inner cylinder 51 is provided with base plate with can be removably mounted
511, base plate 511 closes the lower end of inner cylinder 51, and the inside of inner cylinder 51 passes through the ft connection of steam vent and housing 1, inner cylinder 51
Offered on the wall of side and be covered with silk screen 512 in multiple perforation, and each perforation.React the gas phase for producing laggard through silk screen 512
Enter the inside of inner cylinder 51, and from steam vent discharge, wherein, during gas phase passes through silk screen 512, the drop carried secretly in gas phase
Can be in silk screen 512 be converged into liquid stream and flows back into the reactant in housing 1, so as to reduce the liquid carried secretly when gas phase is discharged
Body, the effectively moisture content of removal gas-phase product, are that downstream dehydration operation reduces pressure, cost-effective.
Further, as shown in Figure 10, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, gas-liquid separator 5
Also include outer barrel 52, outer barrel 52 is set in the outside of inner cylinder 51, and inner cylinder 51 is coaxially disposed with outer barrel 52, inner cylinder 51 and outer barrel 52
Between formed lower ending opening the 3rd ring cavity 54, the upper end of outer barrel 52 is connected with the top inner wall of housing 1, on the inwall of outer barrel 52
Multiple first baffles 521 are provided with, along towards the direction of the axis near inner cylinder 51, each first baffle 521 is by up to having a down dip
Tiltedly, the outer wall of inner cylinder 51 is provided with multiple second baffles 513, along the direction of the axis for being directed away from inner cylinder 51, each second gear
Plate 513 is inclined by up to lower.The setting of first baffle 521 and second baffle 513 is formd equivalent in the 3rd ring cavity 54
Snakelike gas phase channel, when gas phase is moved in the channels, after running into multiple first baffles 521 and second baffle 513, in gas phase
Entrainment a part of drop can be stayed along the gradient of first baffle 521 and second baffle 513, and in gas phase carry secretly it is another
During partial drop can then be assembled at silk screen 512 and be formed and flow back into reactant under liquid flow direction.
Preferably, as shown in Figure 10, the invention provides a kind of aromatic hydrocarbons conversion reactor, wherein, inner cylinder 51 and outer barrel
Connected by many lacing wires 53 between 52.Ensure that inner cylinder 51 is in concentric all the time with outer barrel 52 by setting lacing wire 53, with
Ensure that gas phase can evenly and rapidly be expelled to the outside of housing 1.
The present invention provide aromatic hydrocarbons conversion reactor when in use, gas by air inlet supervisor 21 even into housing 1 inside,
Bottom-up bubbling participates in reaction, and bubble is minute bubbles by meeting is broken after broken bubble component 4 in uphill process, to increase gas
The contact area of bubble and reactant, as the bed temperature that carries out of reaction gradually rises, the relatively low heat transferring medium of temperature is (usually
Cooling water) heat-exchanger rig 3 is entered by heat exchange entrance, after being exchanged heat through 314 and second ring cavity of evaporation tube 313 (cooling water is changed into steam)
It is expelled to outside heat-exchanger rig 3 by heat exchange outlet, takes away heat of reaction, and the liquid product of generation is from the bottom of housing 1 in reactor
The product exit discharge in portion, gas-phase product will enter the gas-liquid separator 5 at the top of housing 1 entrainment of liquid, separate gas after liquid
Phase product is discharged toward downstream from the exhaust outlet at the top of housing 1.
Compared with prior art, advantages of the present invention is as follows：
1st, the present invention provide aromatic hydrocarbons conversion reactor, gas distributor is responsible for by many air inlets, vertical branch pipe and
The setting of arc branch pipe, equally distributed many spray orifices are formed with the bottom of housing, can be in the bottom even of housing
To enclosure interior bubbling, aromatic hydrocarbons, catalyst and oxygen is fully reacted, improve product earning rate.
2nd, the aromatic hydrocarbons conversion reactor that the present invention is provided, air pocket can be pooled by setting broken bubble component in multiple bubbles
When air pocket is broken into minute bubbles, so as to increase the contact area of gas and reactant, so as to improve reaction efficiency.
3rd, the aromatic hydrocarbons conversion reactor that the present invention is provided, can efficiently remove reaction heat, by the heat-exchanging tube bundle being evenly arranged,
Outside the heat for removing reaction, the steam of by-product also is used as steam turbine power generation.
4th, the aromatic hydrocarbons conversion reactor that the present invention is provided, by top gas-liquid separator, effectively removes containing for gas-phase product
Water rate, is that downstream dehydration reduces pressure, cost-effective.
In sum, integral reactor is converted using the new aromatic hydrocarbons of this structure, is had significantly compared with other reactors
Economy.
Schematical specific embodiment of the invention is the foregoing is only, the scope of the present invention is not limited to.It is any
One of ordinary skill in the art, on the premise of design of the invention and principle is not departed from done equivalent variations with repair
Change, the scope of protection of the invention all should be belonged to.
Claims (10)
1. a kind of aromatic hydrocarbons conversion reactor, it is characterised in that the aromatic hydrocarbons conversion reactor includes housing, the inside of the housing
Gas distributor, at least one set of heat-exchanger rig, broken bubble component and gas-liquid separator, the side of the housing are sequentially provided with from the bottom to top
Multiple air admission holes are offered on wall, the air admission hole connects the inside of the gas distributor and the outside of the housing, described
Heat exchange entrance is further opened with the side wall of housing and heat exchange is exported, the heat exchange entrance is changed with described respectively with the heat exchange outlet
Thermal is connected, and steam vent is offered at the top of the housing, and the steam vent is connected with the gas-liquid separator, the shell
The bottom of body offers the product exit that can be opened and closed；
The gas distributor includes many air inlet supervisors, and each air inlet supervisor radially extends setting along the housing,
Each air inlet supervisor includes a blind end and an open end, and the open end is through in multiple air admission holes
The individual outside for extending out to the housing, and the blind end extends to the center of the radial section of the housing, it is each it is described enter
The lower section connection of gas supervisor is provided with multiple vertical branch pipes for extending axially downward along the housing, under each described air inlet supervisor
Side many vertical branch pipes along the housing radial arrangement, the lower end of each vertical branch pipe connects and is provided with one
Individual arc branch pipe, and the lower surface of each arc branch pipe offers multiple spray orifices.
2. aromatic hydrocarbons conversion reactor according to claim 1, it is characterised in that the broken bubble component includes support frame and many
Individual broken bubble ring, support frame as described above is fixed on the inwall of the housing, and support frame as described above is located at the upper of the gas distributor
Side, multiple broken bubble rings are uniformly distributed on support frame as described above.
3. aromatic hydrocarbons conversion reactor according to claim 2, it is characterised in that the broken bubble ring includes ring frame and position
Disk inside the ring frame, the disk is arranged concentrically with the ring frame, and the disk is outer with the annular
Pass through multiple broken bubble pieces between frame to connect, each broken bubble piece is along the setting that radially extends of the disk, and multiple is described broken
Bubble piece is uniformly distributed between the disk and the ring frame, and is uniformly distributed on the disk and is provided with through hole.
4. aromatic hydrocarbons conversion reactor according to claim 2, it is characterised in that support frame as described above includes the first ring, second
Ring and multiple gussets, first ring are fixed on the inwall of the housing by the gusset, and second ring is located at described
The inside of the first ring, is uniformly distributed between first ring and the inwall of the housing and is provided with multiple broken bubble rings, and described
Be uniformly distributed between first ring and second ring and be provided with multiple broken bubble rings, it is each it is described it is broken bubble ring by the gusset with it is described
The inwall connection of the first ring, second ring and/or the housing, is connected with respectively on first ring and second ring
Multiple positioning pipes, the lower end of the heat-exchanger rig is positioned in inserting multiple positioning pipes.
5. aromatic hydrocarbons conversion reactor according to claim 1, it is characterised in that the heat-exchanger rig includes multigroup heat exchanger tube
Beam and set pipe fitting, the set pipe fitting include cooling water concetrated pipe, steam set pipe and two plugging sheets, two closure
Piece closes off the two ends of the steam set pipe, and the cooling water concetrated pipe is located at the inside of the steam set pipe, and institute
State steam set pipe to be coaxially disposed with the cooling water concetrated pipe, the two ends of the cooling water concetrated pipe block with described in two respectively
Piece is tightly connected, and the first closed ring cavity, the cooling water are formed between the cooling water concetrated pipe and the steam set pipe
The inside of concetrated pipe is connected by pipeline with the heat exchange entrance, and first ring cavity is connected by pipeline with the heat exchange outlet
Logical, the heat-exchanging tube bundle is connected with the inside of first ring cavity and the cooling water concetrated pipe.
6. aromatic hydrocarbons conversion reactor according to claim 5, it is characterised in that the heat-exchanging tube bundle includes inner tube and set
Outer tube on the outside of said inner tube, said inner tube is set with the outer coaxial tube, is formed between said inner tube and the outer tube
Second ring cavity, the upper end of said inner tube sequentially through the steam set pipe and the cooling water concetrated pipe and with the cooling water
The inside connection of concetrated pipe, the lower end of said inner tube extends downward at the lower end of the outer tube and connects with second ring cavity
Logical, the lower end of the outer tube is sealed by end socket, and the upper end of the outer tube stretches to described first through the steam set pipe
In ring cavity, first ring cavity is connected with second ring cavity.
7. aromatic hydrocarbons conversion reactor according to claim 6, it is characterised in that the heat-exchanging tube bundle also includes many evaporations
Pipe, many evaporation tubes are parallel with the outer tube, and many evaporation tubes are uniformly distributed in around the outer tube, often
The upper end of evaporation tube described in root connects through the upper end side wall of the outer tube with second ring cavity, and the every evaporation tube
Lower end connected with second ring cavity through the bottom side of the wall of the outer tube.
8. aromatic hydrocarbons conversion reactor according to claim 1, it is characterised in that the gas-liquid separator includes inner cylinder, institute
The upper end and the top inner wall of the housing for stating inner cylinder are tightly connected, and the lower end of the inner cylinder is provided with base plate, institute in which can be removably mounted
The lower end that base plate closes the inner cylinder is stated, the inside of the inner cylinder passes through the ft connection of the steam vent and the housing, institute
State and multiple perforation are offered on the side wall of inner cylinder, and silk screen is covered with each perforation.
9. aromatic hydrocarbons conversion reactor according to claim 8, it is characterised in that the gas-liquid separator also includes outer barrel,
The outer barrel is set in the outside of the inner cylinder, and the inner cylinder is coaxially disposed with the outer barrel, the inner cylinder and the outer barrel
Between form the 3rd ring cavity, the upper end of the outer barrel be connected with the top inner wall of the housing, multiple on the inwall of the outer barrel
First baffle, along towards the direction of the axis near the inner cylinder, each first baffle is inclined by up to lower, described interior
The outer wall of cylinder is provided with multiple second baffles, and along the direction of the axis for being directed away from the inner cylinder, each second baffle is equal
From top to bottom incline.
10. aromatic hydrocarbons conversion reactor according to claim 9, it is characterised in that lead between the inner cylinder and the outer barrel
Excessive root lacing wire connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710091559.3A CN106861590B (en) | 2017-02-20 | 2017-02-20 | Aromatic hydrocarbon conversion reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710091559.3A CN106861590B (en) | 2017-02-20 | 2017-02-20 | Aromatic hydrocarbon conversion reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106861590A true CN106861590A (en) | 2017-06-20 |
| CN106861590B CN106861590B (en) | 2023-05-19 |
Family
ID=59166670
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710091559.3A Active CN106861590B (en) | 2017-02-20 | 2017-02-20 | Aromatic hydrocarbon conversion reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106861590B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109052318A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109261082A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN113694567A (en) * | 2021-09-15 | 2021-11-26 | 中国石油大学(华东) | Two-stage gas-liquid mixing conical helical field separation device and online control system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1685477A1 (en) * | 1989-04-18 | 1991-10-23 | Предприятие П/Я М-5364 | Gas lift unit |
| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN102203222A (en) * | 2009-12-25 | 2011-09-28 | 北京航天万源煤化工工程技术有限公司 | Highly efficient and clean gasification apparatus for carbonaceous dry powder and method thereof |
| CN203663810U (en) * | 2013-12-31 | 2014-06-25 | 北京石油化工工程有限公司 | Three-phase slurry-bed heat taking unit |
| CN205627345U (en) * | 2016-04-16 | 2016-10-12 | 杭州纳生塔内件有限公司 | Binary channels combination formula gas -liquid separation tower |
| CN206508988U (en) * | 2017-02-20 | 2017-09-22 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
-
2017
- 2017-02-20 CN CN201710091559.3A patent/CN106861590B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1685477A1 (en) * | 1989-04-18 | 1991-10-23 | Предприятие П/Я М-5364 | Gas lift unit |
| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN102203222A (en) * | 2009-12-25 | 2011-09-28 | 北京航天万源煤化工工程技术有限公司 | Highly efficient and clean gasification apparatus for carbonaceous dry powder and method thereof |
| CN203663810U (en) * | 2013-12-31 | 2014-06-25 | 北京石油化工工程有限公司 | Three-phase slurry-bed heat taking unit |
| CN205627345U (en) * | 2016-04-16 | 2016-10-12 | 杭州纳生塔内件有限公司 | Binary channels combination formula gas -liquid separation tower |
| CN206508988U (en) * | 2017-02-20 | 2017-09-22 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109052318A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109261082A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109052318B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN113694567A (en) * | 2021-09-15 | 2021-11-26 | 中国石油大学(华东) | Two-stage gas-liquid mixing conical helical field separation device and online control system |
| CN113694567B (en) * | 2021-09-15 | 2022-10-28 | 中国石油大学(华东) | Two-stage gas-liquid mixing conical spiral field separation device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106861590B (en) | 2023-05-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105457563B (en) | Isothermal shift reactor with built-in tube bundle | |
| CN207153662U (en) | A kind of isothermal change furnace | |
| CN106861590A (en) | Aromatic hydrocarbons conversion reactor | |
| CN203990548U (en) | radial parallel catalytic reactor | |
| CN204933425U (en) | A kind of calandria type fixed bed reactor of benzene oxidatoin cis-butenedioic anhydride | |
| CN206508988U (en) | Aromatic hydrocarbons conversion reactor | |
| CN202522106U (en) | Heat exchanger | |
| CN105883852B (en) | A kind of ammonia synthesis reaction system and ammonia synthesis reaction method | |
| CN210346439U (en) | Multi-stage separated plate-fin heat exchanger | |
| CN105413592B (en) | A kind of combined type fixed bed reactors and the device formed by it | |
| CN105043142B (en) | A kind of solids cooler | |
| CN106610237A (en) | Novel carbon dioxide cooling device | |
| CN215855992U (en) | High-efficiency energy-saving distillation device | |
| CN206531413U (en) | A kind of multi-functional cracking rapid-cooling heat exchanger | |
| CN206073772U (en) | A kind of high-performance heat exchanger | |
| CN212263213U (en) | Fluidized reaction system | |
| CN201510870U (en) | Single pump circulation multitubular fixed bed reactor | |
| CN209612901U (en) | A kind of double water cooling horizontal reactors of isothermal uniform flow | |
| CN207019513U (en) | Lamella heat exchanger | |
| CN209043091U (en) | Granular solids cooler | |
| CN212102004U (en) | Collector for fumed silica reaction | |
| CN107398237A (en) | A kind of cold shock formula reactor | |
| CN201684584U (en) | Vinyl acetate reactor | |
| CN108421502B (en) | Spiral-disk type gas distributor and reactor using same | |
| CN202570157U (en) | Straight tube heat exchange type high-efficiency polymerization reaction kettle |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |