CN108654522A - A kind of coil jacket formula axial flow reactor - Google Patents
A kind of coil jacket formula axial flow reactor Download PDFInfo
- Publication number
- CN108654522A CN108654522A CN201810588670.8A CN201810588670A CN108654522A CN 108654522 A CN108654522 A CN 108654522A CN 201810588670 A CN201810588670 A CN 201810588670A CN 108654522 A CN108654522 A CN 108654522A
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- China
- Prior art keywords
- tube sheet
- flat tube
- header
- heat exchange
- cylinder
- Prior art date
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000003054 catalyst Substances 0.000 claims abstract description 44
- 230000008439 repair process Effects 0.000 claims description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical group [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical group [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims 1
- 229910052802 copper Inorganic materials 0.000 claims 1
- 239000010949 copper Substances 0.000 claims 1
- 229910052759 nickel Inorganic materials 0.000 claims 1
- 229910052763 palladium Inorganic materials 0.000 claims 1
- 238000004939 coking Methods 0.000 abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 43
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 30
- 238000006243 chemical reaction Methods 0.000 description 9
- 238000005984 hydrogenation reaction Methods 0.000 description 8
- 238000011068 loading method Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 230000008646 thermal stress Effects 0.000 description 3
- 206010011906 Death Diseases 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 206010020843 Hyperthermia Diseases 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 201000003478 cholangiolocellular carcinoma Diseases 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000008030 elimination Effects 0.000 description 2
- 238000003379 elimination reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 125000003827 glycol group Chemical group 0.000 description 2
- 230000036031 hyperthermia Effects 0.000 description 2
- BLLFVUPNHCTMSV-UHFFFAOYSA-N methyl nitrite Chemical compound CON=O BLLFVUPNHCTMSV-UHFFFAOYSA-N 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- 241000270295 Serpentes Species 0.000 description 1
- 238000010685 alcohol synthesis reaction Methods 0.000 description 1
- 230000006315 carbonylation Effects 0.000 description 1
- 238000005810 carbonylation reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 235000019441 ethanol Nutrition 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002940 palladium Chemical class 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000035882 stress Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
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
- 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
-
- 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
- B01J8/0278—Feeding reactive fluids
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
Abstract
The invention discloses a kind of coil jacket formula axial flow reactors, the upper cover and low head are separately fixed at the top and bottom of cylinder, the snakelike heat exchange tube is distributed along the axial direction of cylinder, the upper flat tube sheet header is connected to the water outlet of snakelike heat exchange tube, the lower flat tube sheet header is connected to the water inlet end of snakelike heat exchange tube, the upper flat tube sheet header is connected to the header tank, the lower flat tube sheet header is connected to the diversion box, the upper flat tube sheet header is supported on the upper and lower part of cylinder with lower flat tube sheet header respectively, the both ends of the center fixed cylinder are separately fixed on flat tube sheet header and lower flat tube sheet header, water leg inner panel being wrapped on snakelike heat exchange tube along snakelike heat exchange tube outer wall, there is the water leg space for flowing water between the water leg inner panel and cylinder.The scheme that the present invention is coordinated using water leg and snakelike heat exchange tube, it can be ensured that entire catalyst bed is all uniformly cooled, and overtemperature coking will not occur.
Description
Technical field
The present invention relates to a kind of chemical reactor more particularly to a kind of coil jacket formula axial flow reactors.
Background technology
Existing hydrogenation reactor is generally shell and tube reactor or plate-type reactor, and shell and tube reactor manages interior filling
Outer catalyst, pipe are water.The tubulation of hydrogenation reactor isThe maximum production to have put into operation on the market at present
Can be 100,000 tons of ethylene glycol, hydrogenation reactor specification is accomplishedSpecification, because thermal stress eliminate it is not thorough
Bottom, bed resistance is high, and reactor leakage, device is in end-of-life state.The ethylene glycol dress that many places are put into operation on the market
It sets, practical monosystem is classified as 50,000 tons of ethylene glycol production capacity, and the hydrogenation reaction of 200,000 tons of ethylene glycol uses two series, fourHIt urges=6000 hydrogenation reactor parallel running, that there are Catalyst packings is few, big, energy consumption of moving thermal energy force difference, resistance
High, the defects of side reaction object is more, device is difficult to amplify；Leak water in the plate of board-like hydrogenation reactor, plate outer loading catalyst, gas
For full Radial Flow, it can theoretically meet device enlargement glycol unit, being not suitable for hydrogenation reaction on Practical Project uses.
It is reacted since with ethylene glycol carburetting can occur for ethyl alcohol, if bed overtemperature occurs and is easy to form coking.
It is enclosed by the cuboid plate of several 150~400 (plate is wide) × H (plate is high) when the heat exchange element of board-like hydrogenation reactor
At periphery, this periphery is really one polygonal, and it is even that catalyst will appear became uneven, is easy to happen catalyst bed
There is coking phenomenon in hot-spot, has no idea to put into actual operation.
Existing oxonation device is generally shell and tube reactor or plate-type reactor, and shell and tube reactor manages interior filling
Outer catalyst, pipe are water.The tubulation of oxonation device isThe maximum production to have put into operation on the market at present
Can be 100,000 tons of ethylene glycol, oxonation device specification is accomplishedSpecification, because thermal stress elimination be not thorough,
Bed resistance is high, and reactor leakage, device is in end-of-life state.The glycol unit that many places are put into operation on the market,
Practical monosystem is classified as 50,000 tons of ethylene glycol production capacity, and the oxonation of 200,000 tons of ethylene glycol uses two series, four
HIt urges=6000 oxonation device parallel running, few, shifting thermal energy force difference that there are Catalyst packings, resistance is big, high energy consumption, is easy hair
Raw decomposition explosion, the defects of side reaction object is more, tube sheet is easily burnt, device is difficult to amplify；
It is enclosed by the cuboid plate of several 150~400 (plate is wide) × H (plate is high) when the heat exchange element of board-like oxonation device
At periphery, this periphery is really one polygonal, and it is even that catalyst will appear became uneven, is easy to happen catalyst bed
Hot-spot is not suitable for oxonation on Practical Project and uses, due to methyl nitrite begin at 140 DEG C thermal decomposition occurs it is anti-
It answers, methyl nitrite will occur to thermally decompose completely at 155~160 DEG C, and pyrolysis occurs to release heat big
(3216j/gCH3ONO), while being a volume increase reaction (2CH3ONO→CH3OH+CH2O+2NO), lead to temperature and pressure
It quickly increases, is bound to cause accident.
Existing methanol reactor is generally shell and tube reactor, plate-type reactor or the reaction of small tube sheet header tube beam formula
Device, shell and tube reactor, it is water that it is outer, which to manage interior loading catalyst, pipe,.The tubulation of methanol synthesis reactor isThe methanol that the maximum production capacity to have put into operation on the market at present is 400,000 tons, methanol synthesis reactor rule
Lattice are accomplishedSpecification, because thermal stress elimination is not thorough, bed resistance is high, reactor leakage, shell and tube first
Alcohol synthesis reaction device can not meet enlarged methanol synthesizer.The country is in the enlarged methanol device of operation, single series production capacity
It it is 60 or 900,000 tons, reactor is the board-like methanol synthesis reactors of Ka Sali or wears the small tube sheet header tube beam formula methanol-fueled CLC of dimension
Reactor, enlarged methanol reactor market are monopolized by foreign technology quotient.But it is anti-that the country introduces the board-like methanol-fueled CLCs of Ka Sali
Nine sets of device is answered, there are six sets of leakages (such as the Inner Mongol long the safe energy, Anhui Hua Yi, the new new energy in Inner Mongol), overhauls plate heat exchanger
Catalysis must be drawn off when element leak source, the repair time is at one month or more.The small tube sheet header tube beam formula methanol for wearing dimension closes
Ten sets or more are introduced at the reactor country, stringing difficulty is big, and the small side reaction object of heat exchange area is more, and catalyst bed overtemperature is (such as god
The methanol synthesis reactor of magnificent packet header methanol-to-olefins project), enlarged device is run using two more parallels, separate unit methanol
Synthesis reactor is difficult to realize enlargement.
Invention content
Technical problem to be solved by the present invention lies in：The easy temperature in the edge of existing serpentine heat exchanger is excessively high, provides
A kind of coil jacket formula axial flow reactor.
The present invention is to solve above-mentioned technical problem by the following technical programs, and the present invention includes cylinder, upper cover, lower envelope
Head, water leg inner panel, snakelike heat exchange tube, upper flat tube sheet header, header tank, lower flat tube sheet header, diversion box, center fixed cylinder；
The upper cover and low head are separately fixed at the top and bottom of cylinder, and the snakelike heat exchange tube is distributed along the axial direction of cylinder,
The upper flat tube sheet header is connected to the water outlet of snakelike heat exchange tube, the water inlet end of lower flat the tube sheet header and snakelike heat exchange tube
Connection, the upper flat tube sheet header is connected to the header tank, and the lower flat tube sheet header is connected to the diversion box, it is described on
Flat tube sheet header is supported on the upper and lower part of cylinder with lower flat tube sheet header respectively, and the both ends of the center fixed cylinder are solid respectively
It is scheduled on flat tube sheet header and lower flat tube sheet header, the water leg inner panel is wrapped in snakelike change along snakelike heat exchange tube outer wall
There is the water leg space for flowing water, the top in the water leg space on heat pipe, between the water leg inner panel and cylinder
It is connected to header tank, bottom is connected to diversion box.
The repair manhole passed in and out for maintenance personal is provided on the upper cover.Repair can easily be entered, do not had to
Upper cover is opened, repair complexity is reduced.
It is provided with gas feed on the upper cover, gas-collecting cap and gas vent, the collection are provided on the low head
Gas cap is connected to gas vent.
It is provided with water outlet on the header tank, water inlet is provided on the diversion box.Realize waterway circulating.
It is filled with catalyst between the water leg inner panel, snakelike heat exchange tube, upper flat tube sheet header and lower flat tube sheet header.
The catalyst is palladium series catalyst.It can be used for ethylene glycol oxonation.
The catalyst is Cu-series catalyst.It can be used for methanol reaction.
The catalyst is nickel catalyst.It can be used for methanation reaction.
Catalyst self-unloading mouth is provided on the low head.Handling for catalyst.
The present invention uses snakelike heat exchange tube for main heat-exchanging tube bundle, and snakelike heat exchange tube thoroughly eliminates heat axially and radially upper
Stress；Use coiled pipe for main heat-exchanging tube bundle, flat outside water-intake pipe in pipe, gas flow direction is vertical configuration with water flowing direction
State；Use coiled pipe for main heat-exchanging tube bundle, gas is axial flowing from top to bottom, manages the outer loading catalyst of interior water-intake pipe, catalysis
Agent loadings are more, it is strong to move thermal energy power；Service personnel can enter reactor by repair manhole and repair.Due to snakelike heat exchange
Pipe is being that no cooling water is cooled down close to the edge of cylinder, is easy to be formed high temperature, and water leg inner panel using the present invention
A water leg space is formed with cylinder, can ensure there is water flowing cooling, avoids leading to urging close to cylinder because of localized hyperthermia
Agent temperature is excessively high.
In entire reaction process, waterway channel is：Flat tube sheet header-snakelike heat exchange tube-is above flat under water inlet-diversion box-
Tube sheet header-header tank-water outlet.
Water leg space is formed between water leg inner panel and cylinder, inside has flow to lead to, water leg inner panel internal edge
Catalyst can be cooling under recirculated water effect, and hot-spot will not occur.
The present invention has the following advantages compared with prior art：The side that the present invention is coordinated using water leg and snakelike heat exchange tube
Case, it can be ensured that entire catalyst bed is all uniformly cooled, and coking will not occur.Waterway circulating is Natural Circulation, is effectively shut out
Oxonation device occurs in unexpected have a power failure for exhausted existing forced circulation oxonation device and the accident of carbonylation system explosion occurs,
Prevent existing forced circulation methanol reaction or methanation reaction device simultaneously and catalyst bed overtemperature knot occurs in unexpected have a power failure
The accidents such as coke.
Description of the drawings
Fig. 1 is the structural schematic diagram of the present invention.
Specific implementation mode
It elaborates below to the embodiment of the present invention, the present embodiment is carried out lower based on the technical solution of the present invention
Implement, gives detailed embodiment and specific operating process, but protection scope of the present invention is not limited to following implementation
Example.
As shown in Figure 1, the present embodiment include cylinder 1, upper cover 2, low head 3, water leg inner panel 4, snakelike heat exchange tube 5,
Upper flat tube sheet header 6, header tank 7, lower flat tube sheet header 8, diversion box 9, center fixed cylinder 10；The upper cover 2 and low head 3
The top and bottom of cylinder 1 are separately fixed at, the snakelike heat exchange tube 5 is along the axial direction distribution of cylinder 1, the upper flat tube sheet header
6 are connected to the water outlet of snakelike heat exchange tube 5, and the lower flat tube sheet header 8 is connected to the water inlet end of snakelike heat exchange tube 5, it is described on
Flat tube sheet header 6 is connected to the header tank 7, and the lower flat tube sheet header 8 is connected to the diversion box 9, the upper flat tube sheet
Header 6 is supported on the upper and lower part of cylinder 1 with lower flat tube sheet header 8 respectively, and the both ends of the center fixed cylinder 10 are solid respectively
It is scheduled on flat tube sheet header 6 and lower flat tube sheet header 8, the water leg inner panel 4 is wrapped in snake along 5 outer wall of snakelike heat exchange tube
Have the water leg space 11 for flowing water, the water leg empty on shape heat exchanger tube 5, between the water leg inner panel 4 and cylinder 1
Between 11 top be connected to header tank 7, bottom be connected to diversion box 9.The dimension passed in and out for maintenance personal is provided on the upper cover 2
Manhole 12 is repaiied, repair can be easily entered, does not have to open upper cover 2, reduces repair complexity.It is arranged on the upper cover 2
There is gas feed 13, gas-collecting cap 14 and gas vent 15 are provided on the low head 3, the gas-collecting cap 14 is connected to gas vent
15.It is provided with water outlet 16 on the header tank 7, water inlet 19 is provided on the diversion box 9.Realize waterway circulating.It is described
It is filled with catalyst 17 between water leg inner panel 4, snakelike heat exchange tube 5, upper flat tube sheet header 6 and lower flat tube sheet header 8.It is described to urge
Agent 17 is palladium series catalyst.It can be used for ethylene glycol oxonation.The catalyst 17 is Cu-series catalyst.It is anti-to can be used for methanol
It answers.The catalyst 17 is nickel catalyst.It can be used for methanation reaction.Catalyst self-unloading mouth is provided on the low head 3
18.Handling for catalyst 17.
Use snakelike heat exchange tube 5 for main heat-exchanging tube bundle, snakelike heat exchange tube 5 is answered in axially and radially upper heat of thoroughly eliminating
Power；Use coiled pipe for main heat-exchanging tube bundle, flat outside water-intake pipe in pipe, gas flow direction is vertical configuration with water flowing direction
State；It uses coiled pipe for main heat-exchanging tube bundle, manages the outer loading catalyst of interior water-intake pipe, 17 loadings of catalyst are more, it is strong to move thermal energy power；
Service personnel can be repaired by repairing manhole 12 into reactor, and coiled pipe is completed under the premise of not drawing off catalyst 17
Weld seam overhauls.Since snakelike heat exchange tube 5 is being that no cooling water is cooled down close to the edge of cylinder 1, it is easy to form high temperature, and
Water leg inner panel 4 using the present invention forms a water leg space 11 with cylinder 1, can ensure there is water flowing cooling, avoid
Because localized hyperthermia causes 17 temperature of catalyst close to cylinder 1 excessively high.
In entire reaction process, waterway channel is：Flat tube sheet header 8- snakelike heat exchange tubes 5- under water inlet 19- diversion boxs 9-
Upper flat tube sheet header 6- header tank 7- water outlets 16.
Water leg space 11 is formed between water leg inner panel 4 and cylinder 1, inside has flow to lead to, 4 internal edges of water leg inner panel
The catalyst 17 of edge can be cooling under recirculated water effect, and hot-spot will not occur.Center fixed cylinder 10 plays fixed bearing
Effect, effectively the whole bearing of snakelike heat exchange tube 5 can be got up.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
All any modification, equivalent and improvement etc., should all be included in the protection scope of the present invention made by within refreshing and principle.
Claims (9)
1. a kind of coil jacket formula axial flow reactor, which is characterized in that including cylinder, upper cover, low head, water leg inner panel,
Snakelike heat exchange tube, upper flat tube sheet header, header tank, lower flat tube sheet header, diversion box, center fixed cylinder；The upper cover is under
End socket is separately fixed at the top and bottom of cylinder, and the snakelike heat exchange tube is distributed along the axial direction of cylinder, the upper flat tube sheet connection
Case is connected to the water outlet of snakelike heat exchange tube, and the lower flat tube sheet header is connected to the water inlet end of snakelike heat exchange tube, described flat
Tube sheet header is connected to the header tank, and the lower flat tube sheet header is connected to the diversion box, the upper flat tube sheet header with
Under flat tube sheet header be supported on the upper and lower part of cylinder respectively, the both ends of the center fixed cylinder are separately fixed at flat tube sheet
On header and lower flat tube sheet header, water leg inner panel being wrapped on snakelike heat exchange tube along snakelike heat exchange tube outer wall is described
There is the water leg space for flowing water, the top in the water leg space to be connected to header tank between water leg inner panel and cylinder,
Bottom is connected to diversion box.
2. a kind of coil jacket formula axial flow reactor according to claim 1, which is characterized in that be arranged on the upper cover
It is useful for the repair manhole of maintenance personal's disengaging.
3. a kind of coil jacket formula axial flow reactor according to claim 1, which is characterized in that be arranged on the upper cover
There is gas feed, gas-collecting cap and gas vent are provided on the low head, the gas-collecting cap is connected to gas vent.
4. a kind of coil jacket formula axial flow reactor according to claim 1, which is characterized in that be arranged on the header tank
There is water outlet, water inlet is provided on the diversion box.
5. a kind of coil jacket formula axial flow reactor according to claim 1, which is characterized in that the water leg inner panel,
It is filled with catalyst between snakelike heat exchange tube, upper flat tube sheet header and lower flat tube sheet header.
6. a kind of coil jacket formula axial flow reactor according to claim 5, which is characterized in that the catalyst is palladium system
Catalyst.
7. a kind of coil jacket formula axial flow reactor according to claim 5, which is characterized in that the catalyst is copper system
Catalyst.
8. a kind of coil jacket formula axial flow reactor according to claim 5, which is characterized in that the catalyst is nickel system
Catalyst.
9. a kind of coil jacket formula axial flow reactor according to claim 5, which is characterized in that be arranged on the low head
There is catalyst self-unloading mouth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810588670.8A CN108654522A (en) | 2018-06-08 | 2018-06-08 | A kind of coil jacket formula axial flow reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810588670.8A CN108654522A (en) | 2018-06-08 | 2018-06-08 | A kind of coil jacket formula axial flow reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108654522A true CN108654522A (en) | 2018-10-16 |
Family
ID=63775542
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810588670.8A Pending CN108654522A (en) | 2018-06-08 | 2018-06-08 | A kind of coil jacket formula axial flow reactor |
Country Status (1)
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111821924A (en) * | 2020-07-13 | 2020-10-27 | 江苏永大化工机械有限公司 | DMO reactor |
| CN112337409A (en) * | 2020-11-25 | 2021-02-09 | 重庆华峰化工有限公司 | Production system of hexamethylene diamine |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5470542A (en) * | 1993-06-30 | 1995-11-28 | Sulzer Chemtech Ag | Catalyzing fixed bed reactor |
| CN103240035A (en) * | 2012-02-10 | 2013-08-14 | 杭州林达化工技术工程有限公司 | Gas-solid phase catalytic reactor |
| CN105642197A (en) * | 2014-09-24 | 2016-06-08 | 楼韧 | Large-sized reactor, and device and process thereof |
| CN107830750A (en) * | 2017-09-27 | 2018-03-23 | 兰州兰石集团有限公司 | Coal gasifier ash-dregs cooler |
| CN208742509U (en) * | 2018-06-08 | 2019-04-16 | 南京敦先化工科技有限公司 | A kind of water-cooled snakelike heat exchange tube axial flow reactor |
-
2018
- 2018-06-08 CN CN201810588670.8A patent/CN108654522A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5470542A (en) * | 1993-06-30 | 1995-11-28 | Sulzer Chemtech Ag | Catalyzing fixed bed reactor |
| CN103240035A (en) * | 2012-02-10 | 2013-08-14 | 杭州林达化工技术工程有限公司 | Gas-solid phase catalytic reactor |
| CN105642197A (en) * | 2014-09-24 | 2016-06-08 | 楼韧 | Large-sized reactor, and device and process thereof |
| CN107830750A (en) * | 2017-09-27 | 2018-03-23 | 兰州兰石集团有限公司 | Coal gasifier ash-dregs cooler |
| CN208742509U (en) * | 2018-06-08 | 2019-04-16 | 南京敦先化工科技有限公司 | A kind of water-cooled snakelike heat exchange tube axial flow reactor |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111821924A (en) * | 2020-07-13 | 2020-10-27 | 江苏永大化工机械有限公司 | DMO reactor |
| CN112337409A (en) * | 2020-11-25 | 2021-02-09 | 重庆华峰化工有限公司 | Production system of hexamethylene diamine |
| CN112337409B (en) * | 2020-11-25 | 2024-02-06 | 重庆华峰化工有限公司 | Production system of hexamethylenediamine |
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Application publication date: 20181016 |