CN206500146U - A kind of spherical cavity header coil pipe reactor of water route Natural Circulation - Google Patents
A kind of spherical cavity header coil pipe reactor of water route Natural Circulation Download PDFInfo
- Publication number
- CN206500146U CN206500146U CN201720089704.XU CN201720089704U CN206500146U CN 206500146 U CN206500146 U CN 206500146U CN 201720089704 U CN201720089704 U CN 201720089704U CN 206500146 U CN206500146 U CN 206500146U
- Authority
- CN
- China
- Prior art keywords
- pipe
- header
- spherical cavity
- water
- reactor
- 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.)
- Active
Links
Abstract
The utility model discloses a kind of spherical cavity header coil pipe reactor of water route Natural Circulation, including pressure-bearing shell, catalyst framework and heat-exchanging tube bundle, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes outlet pipe, spherical cavity of catchmenting header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe is arranged on the top of pressure-bearing shell, one end of the spherical cavity header that catchments connects the import of outlet pipe, the other end is connected by branch pipe with the outlet of coiled pipe, axial direction distribution of the coiled pipe along pressure-bearing shell, one end of described point of water polo chamber header connects the import of coiled pipe by branch pipe, and the other end connects the outlet of water inlet pipe, and the water inlet pipe is connected to the bottom of pressure-bearing shell.The utility model thoroughly eliminates thermal stress, effectively improves the security and stability of carbonylation, hydrogenation, methanol synthesis reactor, is prevented effectively from the defect such as easy leakage of heat exchanger plates in the easy leakage of shell and tube reactor in the prior art and plate-type reactor.
Description
Technical field
The utility model is related to a kind of chemical reactor, more particularly to a kind of water route Natural Circulation spherical cavity header snake
Tubular reactor.
Background technology
Existing hydrogenation reactor is generally in shell and tube reactor or plate-type reactor, shell and tube reactor, pipe and loaded
Outer catalyst, pipe are water.The tubulation of hydrogenation reactor is 45 × 4~φ of φ 70 × 4, the maximum production commercially put into operation at present
Energy is 100,000 tons of ethylene glycol, and hydrogenation reactor specification accomplishes φ 6800HUrge=10000 specification, because thermal stress eliminates not thorough
Bottom, bed resistance is high, and reactor leakage, device is in end-of-life state.The ethylene glycol dress that commercially many places are put into operation
Put, actual monosystem is classified as 50,000 tons of ethylene glycol production capacity, and the hydrogenation reaction of 200,000 tons of ethylene glycol is using two series, four φ
4200、HUrge=6000 hydrogenation reactor parallel running, have that Catalyst packing is few, big, high energy consumption of moving hot ability, resistance,
The defect such as side reaction thing is more, device is difficult to amplify；Leak water in the plate of board-like hydrogenation reactor, the outer loading catalyst of plate, gas are
Full Radial Flow, can meet unsuitable hydrogenation reaction on larger-scale unit glycol unit, Practical Project and use in theory.By
Can occur carburetting reaction in ethanol and ethylene glycol, if bed overtemperature occurs and easily forms coking.
Enclosed during the heat exchange element of board-like hydrogenation reactor by several 150~400 (plate is wide) × H (plate is high) cuboid plate
Into periphery, this periphery is really one polygonal, and catalyst occurs that became uneven is even, easily occurs beds
, there is coking phenomenon in hot-spot, the actual operation of input of having no idea.
Existing oxonation device is generally in shell and tube reactor or plate-type reactor, shell and tube reactor, pipe and loaded
Outer catalyst, pipe are water.The tubulation of oxonation device is 25 × 2~φ of φ 32 × 2, the maximum production commercially put into operation at present
Energy is 100,000 tons of ethylene glycol, and oxonation device specification accomplishes φ 6000HUrge=8000 specification, because thermal stress eliminates not thorough,
Bed resistance is high, and reactor leakage, device is in end-of-life state.The glycol unit that commercially many places are put into operation,
Actual monosystem is classified as 50,000 tons of ethylene glycol production capacity, the oxonation of 200,000 tons of ethylene glycol using two series, four φ 4600,
HUrge, there is few Catalyst packing, the hot ability of shifting, big resistance, easily high energy consumption, hair in=6000 oxonation device parallel running
Raw decomposition explosion, the defect such as side reaction thing is more, tube sheet easily burns, device is difficult to amplify；
Enclosed during the heat exchange element of board-like oxonation device by several 150~400 (plate is wide) × H (plate is high) cuboid plate
Into periphery, this periphery is really one polygonal, and catalyst occurs that became uneven is even, easily occurs beds
Be not suitable for oxonation on hot-spot, Practical Project to use, because methyl nitrite begins to occur thermal decomposition instead at 140 DEG C
Should, complete thermal decomposition will occur for methyl nitrite at 155~160 DEG C, and it is big to occur pyrolysis releasing heat
(3216j/g CH3ONO), while being a volume increase reaction (2CH3ONO→CH3OH+CH2O+2NO), temperature and pressure are caused
Power is quickly raised, and certainly will cause the accident generation.
Existing methanol reactor is generally shell and tube reactor, plate-type reactor or the reaction of small tube sheet header tube beam formula
It is water that loading catalyst, pipe are outer in device, shell and tube reactor, pipe.The tubulation of methanol synthesis reactor be 38 × 2~φ of φ 44 ×
2, the maximum production capacity commercially put into operation at present is 400,000 tons of methanol, and methanol synthesis reactor specification accomplishes φ 4200HUrge=
7000 specification, because thermal stress eliminates not thorough, bed resistance is high, and reactor leakage, shell and tube methanol synthesis reactor is met
Not maximization methanol synthesizer.The domestic maximization methanol device in operation, single series production capacity is 60 or 900,000 tons, reaction
Device is the board-like methanol synthesis reactors of Ka Sali or the small tube sheet header tube beam formula methanol synthesis reactor for wearing dimension, and maximize methanol
Reactor market is monopolized by foreign technology business.But the country introduces board-like nine sets of the methanol synthesis reactors of Ka Sali, has six sets to let out
Dew (the long safe energy in such as Inner Mongol, Anhui Hua Yi, the new new energy in Inner Mongol), will must be urged when overhauling board-like heat exchanger component leak source
Change is drawn off, and the repair time is more than one month.Introduce ten in the small tube sheet header tube beam formula methanol synthesis reactor country for wearing dimension
More than set, stringing difficulty is big, and the small side reaction thing of heat exchange area is more, beds overtemperature (such as Shenhua packet header methanol-to-olefins
Purpose methanol synthesis reactor), maximization device is difficult to using two more parallel operations, separate unit methanol synthesis reactor
Maximization.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art there is provided a kind of spherical cavity of water route Natural Circulation to join
Case coil pipe reactor, stress is eliminated on radial and axial and meets production needs.
The utility model is achieved through the following technical solutions, and the utility model includes pressure-bearing shell, catalyst framework
And heat-exchanging tube bundle, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes water outlet
Manage, spherical cavity of catchmenting header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe is arranged on the top of pressure-bearing shell, described
One end of spherical cavity of catchmenting header connects the import of outlet pipe, and the other end is connected by branch pipe with the outlet of coiled pipe, the coiled pipe edge
The axial direction distribution of pressure-bearing shell, one end of described point of water polo chamber header connects the import of coiled pipe by branch pipe, the other end connect into
The outlet of water pipe, the water inlet pipe is connected to the bottom of pressure-bearing shell.
Maintainer can respectively enter inside point water polo chamber header and catchment spherical cavity header by water inlet pipe and outlet pipe
Inside, completion coiled pipe weld seam maintenance under the premise of catalyst is not drawn off.
The pressure-bearing shell includes upper cover, housing, support platform, low head；The upper cover and housing pass through flange
Connection, the support platform is arranged on low head, and the low head is fixed on the bottom of housing.Pressure-bearing shell is not involved in instead
Should, pressure is primarily subjected to, high-temperature reacting gas is not contacted.
As one of preferred embodiment of the present utility model, the upper cover is provided with thermocouple port, delivery port and upper gas port,
The outlet pipe is arranged in delivery port.
As one of preferred embodiment of the present utility model, the low head is provided with lower gas port, water inlet and catalyst certainly
Unload mouth；The water inlet pipe is arranged in water inlet.
The catalyst framework includes flat cover, outer inflator, interior inflator and chuck；The flat cover is arranged on the spherical cavity header that catchments
Top, the outer inflator is along the axially arranged of housing, and the interior inflator is set in outer inflator, and the coiled pipe is arranged at outer gas
In space between cylinder and interior inflator, there is space, spherical cavity header and point water polo of catchmenting between the outer inflator and housing
Chamber header is separately positioned on the top and bottom of outer inflator, and the chuck is set on point water polo chamber header, the chuck difference
Inflator and lower gas port in connection, described point of water polo chamber header and chuck are supported in support platform, the outlet pipe, flat cover, collection
Loading catalyst in the space that water polo chamber header, outer inflator, coiled pipe, interior inflator, chuck, water inlet pipe are formed.
The catalyst framework also includes airway tube, and the airway tube is connected in lower gas port.
A kind of method that hydrogenation reaction or methanol synthesis reaction are carried out using described reactor.
The method of the hydrogenation reaction or methanol synthesis reaction, comprises the following steps：
(11) copper silicon systems or copper-zinc system catalyst are loaded in catalyst inframe；
(12) leak water from the bottom to top in coiled pipe, upper gas port enters reacting gas, catalyst bed is passed radially through by outer inflator
To interior inflator hydrogenation reaction or methanol synthesis reaction occur for layer；
(13) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe, by the heat after the hydrogenation or methanol synthesis reaction of catalyst inframe
Amount is removed, and gas is then collected by interior inflator, into the annular space of chuck and point water polo chamber header, is then discharged and is taken away through lower gas port
Heat.
A kind of method that oxonation is carried out using described reactor.
The method of the oxonation, comprises the following steps：
(21) palladium series catalyst is loaded in catalyst inframe；
(22) leak water from the bottom to top in coiled pipe, lower gas port enters reacting gas, into the annular space of chuck and point water polo chamber header,
Beds are passed radially through to outer inflator by interior inflator, occur oxonation；
(23) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe removes the heat after the oxonation of catalyst inframe, gas
Then collected by outer inflator, then discharged through upper gas port and take away heat.
The utility model uses coiled pipe for main heat-exchanging tube bundle, and coiled pipe tube bank thoroughly eliminates heat on axially and radially should
Power；Ensure that gas flows radially across beds using outer inflator and interior inflator technology, the bed resistance of oxonation≤
0.001MPa, bed resistance≤0.005MPa of hydrogenation reaction, bed resistance≤0.008MPa of methanol synthesis reaction；Using snake
Manage as main heat-exchanging tube bundle, flat outside water-intake pipe in pipe, gas flow direction is plumbness with water flow direction；Using drum
Waterway circulating between being restrained with coiled pipe is follows naturally, and waterway circulating multiplying power is high；Coiled pipe is used for main heat-exchanging tube bundle and radial direction
Gas distributor technology combines, and loaded catalyst is more, it is strong to move heat energy power；Divided respectively using water inlet pipe and outlet pipe
Sealed inside water polo chamber header with spherical cavity header interior welds of catchmenting, maintainer can respectively be entered by water inlet pipe and outlet pipe
Enter inside point water polo chamber header with inside the spherical cavity header that catchments, the maintenance of coiled pipe weld seam is completed on the premise of catalyst is not drawn off.
The utility model has advantages below compared with prior art：
1st, the utility model coiled pipe tube bank thoroughly eliminates thermal stress on axially and radially, effectively improves carbonylation, hydrogenation, first
The security and stability of alcohol synthesis reaction device, is prevented effectively from the easy leakage of shell and tube reactor in the prior art and plate-type reactor
The defects such as the easy leakage of heat exchanger plates；
2nd, the technology combined using outer inflator and interior inflator ensures that gas flows radially across beds, effectively reduces carbonyl
Ethylene glycol per ton can reduce circulator power consumption in change, hydrogenation reaction and methanol synthesis reaction circulator power consumption, oxonation
It is more than 300KW.h/t ethylene glycol, in hydrogenation reaction ethylene glycol per ton can reduce circulator power consumption 100KW.h/t ethylene glycol with
On, methanol per ton can be reduced more than circulator power consumption 56KW.h/t methanol in methanol synthesis reaction；
3rd, using leaking water, manage flat outside outer loading of catalyst tubes in coiled pipe pipe, Catalyst packing and the very convenient letter of self-unloading
Victory, ensures that gas flows radially across beds, gas flow direction and water flow direction using outer inflator and interior inflator technology
For plumbness；Using coiled pipe and point water polo chamber and a spherical cavity interior welds of catchmenting, realization completes snake under the premise of not drawing off catalyst
Pipe leak source is overhauled；
4th, coiled pipe is used for main heat-exchanging tube bundle, and flat outside water-intake pipe in pipe, water is turbulence state in pipe, and gas side water side is passed
Hot coefficient is high, and gas flow direction is plumbness with water flow direction, and total heat transfer coefficient height shifting heat energy power is strong, accomplishes catalysis
Agent bed is approximate isothermal bed, is prevented effectively from bed overtemperature, coking (hydrogenation reaction), nitrous acid heating thermal decomposition phenomenon (carbonyl
Change reaction) occur and wax deposition (methanol synthesis reaction), prevent security incident；
5th, gas Radial Flow, resistance are low, and loaded catalyst is more, it is strong to move heat energy power, meets ethylene glycol, methanol device big
Typeization needs, the oxonation device or hydrogenation reactor one of 10~300,000 tons of ethylene glycol, and carbonylation/hydrogenation plant is only one
Individual series, can make existing carbonylation/hydrogenation plant floor space reduce by more than 50%, construction investment reduction by more than 50%, operation
Operating cost reduction by more than 40%；900000 tons of methanol devices, one reactor；
6th, the waterway circulating between drum and coiled pipe tube bank is used to prevent existing forced circulation carbonylation for Natural Circulation, effectively
Oxonation device occurs in unexpected have a power failure for reaction unit and the accident of carbonylation system blast occurs, and is followed while preventing existing pressure
In unexpected have a power failure the accidents such as hydrogenation reactor overtemperature coking occur for ring hydrogenation reaction device, it is ensured that maximization methanol synthesizer
Side reaction thing≤1000PPm.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Embodiment
Embodiment of the present utility model is elaborated below, the present embodiment using technical solutions of the utility model before
Put and implemented, give detailed embodiment and specific operating process, but protection domain of the present utility model is not limited
In following embodiments.
Embodiment 1
As shown in figure 1, the present embodiment include pressure-bearing shell, catalyst framework and heat-exchanging tube bundle, the catalyst framework and
Heat-exchanging tube bundle is separately positioned in pressure-bearing shell；The heat-exchanging tube bundle include outlet pipe 4, spherical cavity of catchmenting header 7, coiled pipe 11, point
Water polo chamber header 13 and water inlet pipe 18, the outlet pipe 4 are arranged on the top of pressure-bearing shell, described to catchment the one of spherical cavity header 7
The import of end connection outlet pipe 4, the other end is connected by the outlet of branch pipe and coiled pipe 11, axle of the coiled pipe 11 along pressure-bearing shell
To distribution, one end of described point of water polo chamber header 13 connects the import of coiled pipe 11 by branch pipe, other end connection water inlet pipe 18
Outlet, the water inlet pipe 18 is connected to the bottom of pressure-bearing shell.
Maintainer can respectively enter the inside of point water polo chamber header 13 and spherical cavity of catchmenting by water inlet pipe 18 and outlet pipe 4
Inside header 7, completion coiled pipe 11 weld seam maintenance under the premise of catalyst is not drawn off.
Pressure-bearing shell includes upper cover 5, housing 9, support platform 16, low head 17；The upper cover 5 and housing 9 pass through
Flange 8 is connected, and the support platform 16 is arranged on low head 17, and the low head 17 is fixed on the bottom of housing 9.Pressure-bearing shell
Body is not involved in reaction, is primarily subjected to pressure, does not contact high-temperature reacting gas.
Upper cover 5 is provided with thermocouple port 1, delivery port 2 and upper gas port 3, and the outlet pipe 4 is arranged in delivery port 2；Under
End socket 17 is provided with lower gas port 19, water inlet 20 and catalyst self-unloading mouth 21；The water inlet pipe 18 is arranged in water inlet 20.
The catalyst framework includes flat cover 6, outer inflator 10, interior inflator 12, chuck 14 and airway tube 15；The flat cover 6
The top for the spherical cavity header 7 that catchments is arranged on, the outer inflator 10 is along the axially arranged of housing 9, and the interior inflator 12 is arranged outside
In inflator 10, the coiled pipe 11 is arranged in the space between outer inflator 10 and interior inflator 12, the outer inflator 10 and housing 9 it
Between there is space, it is described to catchment spherical cavity header 7 and point water polo chamber header 13 is separately positioned on the top and bottom of outer inflator 10, institute
State chuck 14 to be set on point water polo chamber header 13, the chuck 14 is respectively communicated with interior inflator 12 and airway tube 15, the air guide
Pipe 15 is connected in lower gas port 19, and described point of water polo chamber header 13 and chuck 14 are supported in support platform 16, the outlet pipe
4th, flat cover 6, spherical cavity of catchmenting header 7, outer inflator 10, coiled pipe 11, interior inflator 12, chuck 14, airway tube 15, water inlet pipe 18 are formed
Loading catalyst in space.
The method that the present embodiment carries out hydrogenation reaction using above-mentioned reactor, comprises the following steps：
(11) copper silicon systems catalyst is loaded in catalyst inframe；
(12) leak water from the bottom to top in coiled pipe 11, upper gas port 3 enters reacting gas, catalysis is passed radially through by outer inflator 10
To interior inflator 12 hydrogenation reaction or methanol synthesis reaction occur for agent bed；
(13) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe 11, after the hydrogenation or methanol synthesis reaction of catalyst inframe
Heat is removed, and gas is then collected by interior inflator 12, into the annular space of chuck 14 and point water polo chamber header 13, is pooled to airway tube
15, then discharged through lower gas port 19 and take away heat.
Hydrogenation reaction is carried out using the reactor of the present embodiment, CH can be completed3OCOCOCH3O+2H2=HOCH2COOCH3+
CH3OH+QPut、HOCH2COOCH3+2H2=HOCH2CH2OH+CH3OH+QPut、HOCH2CH2OH+H2=CH3CH2OH+H2O+QPut、
HOCH2CH2OH+CH3CH2OH=HOCH2C(CH2CH3)HOH+H2O+QPutEtc. hydrogenation reaction, reaction releases heat by coiled pipe 11
Water, which absorbs, removes beds heat, and by-product 1.0~2.5MPa saturated vapors.
Embodiment 2
The method that the present embodiment carries out oxonation using described reactor, comprises the following steps：
(21) palladium series catalyst is loaded in catalyst inframe；
(22) leak water from the bottom to top in coiled pipe 11, lower gas port 19 enters reacting gas, into chuck 14 and a point water polo chamber header
13 annular space, passes radially through beds to outer inflator 10 by interior inflator 12, occurs oxonation；
(23) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe 11 removes the heat after the oxonation of catalyst inframe, gas
Body is then collected by outer inflator 10, is then discharged through upper gas port 3 and is taken away heat.
Using the reactor of the present embodiment, 2CH can be completed3ONO+2CO=CH3OCOCOCH3O+2NO+QPut、2CH3ONO+
CO=CH3OCOCH3O+2NO+QPut、2CH3ONO=HCHO+CH3OH+2NO+QPutDeng oxonation, reaction releases heat by coiled pipe
Water, which absorbs, in 11 removes beds heat, and by-product 0.08~0.12MPa saturated vapors.
The gas of the present embodiment is moved towards with embodiment 1 on the contrary, other embodiment and embodiment 1 are identical.
Embodiment 3
The method that the present embodiment carries out methanol synthesis reaction using described reactor, comprises the following steps：
(31) copper-zinc system catalyst is loaded in catalyst inframe；
(32) leak water from the bottom to top in coiled pipe 11, upper gas port 3 enters reacting gas, catalysis is passed radially through by outer inflator 10
To interior inflator 12 H occurs for agent bed2With CO, CO2Generate CH3OH (methanol) synthetic reaction；
(33) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe 11 moves the heat after the methanol synthesis reaction of catalyst inframe
Go out, gas is then collected by interior inflator 12, into the annular space of chuck 14 and point water polo chamber header 13, be pooled to airway tube 15, then
Discharged through lower gas port 19 and take away heat.
Using the reactor of the present embodiment, 2H can be completed2+ CO=CH3OH+QPut、3H2+CO2=CH3OH+H2O+QPutEtc. first
Alcohol synthesis reaction, reaction releases heat and absorbs removal beds heat by water in coiled pipe 11, and 2.0~3.8MPa of by-product is full
And steam.
Other embodiment and embodiment 1 are identical.
Preferred embodiment of the present utility model is the foregoing is only, it is all at this not to limit the utility model
Any modifications, equivalent substitutions and improvements made within the spirit and principle of utility model etc., should be included in the utility model
Protection domain within.
Claims (6)
1. the spherical cavity header coil pipe reactor of a kind of water route Natural Circulation, it is characterised in that including pressure-bearing shell, catalyst frame
Body and heat-exchanging tube bundle, the catalyst framework and heat-exchanging tube bundle are separately positioned in pressure-bearing shell；The heat-exchanging tube bundle includes
Water pipe, spherical cavity of catchmenting header, coiled pipe, point water polo chamber header and water inlet pipe, the outlet pipe are arranged on the top of pressure-bearing shell, institute
The one end for stating the spherical cavity header that catchments connects the import of outlet pipe, and the other end is connected by branch pipe with the outlet of coiled pipe, the coiled pipe
It is distributed along the axial direction of pressure-bearing shell, one end of described point of water polo chamber header connects the import of coiled pipe, other end connection by branch pipe
The outlet of water inlet pipe, the water inlet pipe is connected to the bottom of pressure-bearing shell.
2. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 1, it is characterised in that institute
Stating pressure-bearing shell includes upper cover, housing, support platform, low head；The upper cover and housing are connected by flange, the branch
Support platform is arranged on low head, and the low head is fixed on the bottom of housing.
3. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 2, it is characterised in that institute
Upper cover is stated provided with thermocouple port, delivery port and upper gas port, the outlet pipe is arranged in delivery port.
4. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 2, it is characterised in that institute
Low head is stated provided with lower gas port, water inlet and catalyst self-unloading mouthful；The water inlet pipe is arranged in water inlet.
5. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 4, it is characterised in that institute
Stating catalyst framework includes flat cover, outer inflator, interior inflator and chuck；The flat cover is arranged on the top for the spherical cavity header that catchments, institute
Outer inflator is stated along the axially arranged of housing, the interior inflator is set in outer inflator, and the coiled pipe is arranged at outer inflator and interior gas
In space between cylinder, there is space, spherical cavity header and point water polo chamber header point of catchmenting between the outer inflator and housing
The top and bottom of outer inflator are not arranged on, and the chuck is set on point water polo chamber header, and the chuck is respectively communicated with interior gas
Cylinder and lower gas port, described point of water polo chamber header and chuck are supported in support platform, the outlet pipe, flat cover, spherical cavity of catchmenting connection
Loading catalyst in the space that case, outer inflator, coiled pipe, interior inflator, chuck, water inlet pipe are formed.
6. a kind of spherical cavity header coil pipe reactor of water route Natural Circulation according to claim 5, it is characterised in that institute
Stating catalyst framework also includes airway tube, and the airway tube is connected in lower gas port.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089704.XU CN206500146U (en) | 2017-01-23 | 2017-01-23 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089704.XU CN206500146U (en) | 2017-01-23 | 2017-01-23 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206500146U true CN206500146U (en) | 2017-09-19 |
Family
ID=59833161
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720089704.XU Active CN206500146U (en) | 2017-01-23 | 2017-01-23 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206500146U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106732311A (en) * | 2017-01-23 | 2017-05-31 | 南京敦先化工科技有限公司 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
-
2017
- 2017-01-23 CN CN201720089704.XU patent/CN206500146U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106732311A (en) * | 2017-01-23 | 2017-05-31 | 南京敦先化工科技有限公司 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106732311A (en) | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation | |
| CN203916626U (en) | A kind of inner/outer drum structure the radial reactor with interpolation pipe heat exchanger | |
| CN100528320C (en) | Transverse pipe type heat transfer reaction unit | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN106582455A (en) | Straight pipe header coil pipe type reactor for waterway natural circulation | |
| CN102160981B (en) | Catalytic reaction equipment | |
| CN206492484U (en) | A kind of straight tube header coil pipe reactor of water route Natural Circulation | |
| CN206500146U (en) | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation | |
| CN104437266B (en) | Phase change heat absorption temperature control reactor | |
| CN102698659B (en) | Methanol synthesis reactor structure | |
| CN204365252U (en) | A kind of large-scale reactor and device thereof | |
| CN208742509U (en) | A kind of water-cooled snakelike heat exchange tube axial flow reactor | |
| CN202516536U (en) | Shift-converter with built-in cold wall | |
| CN201301294Y (en) | Tube array type epoxy ethane reactor with quench zone | |
| CN103241782A (en) | Method for synthesizing nickel carbonyl under medium pressure in rotating kettle | |
| CN203437109U (en) | Full radial direction steam raising type sulfur-resisting conversion reactor | |
| CN201701922U (en) | Catalytic reaction equipment | |
| CN205973791U (en) | Hydrogen peroxide solution production hydrogenation uses novel fixed bed | |
| CN101491751B (en) | Heat-exchange catalytic reaction device | |
| CN108654522A (en) | A kind of coil jacket formula axial flow reactor | |
| CN102705801B (en) | High-temperature vertical waste heat boiler with coil pipes | |
| CN104368282A (en) | Bundle tube type water bed reactor | |
| CN103585933A (en) | Corrugated board type uniform-temperature hydrogenation reactor | |
| CN216538373U (en) | Final stage water transfer heat bed layer ammonia synthesis reactor | |
| CN113091338B (en) | Reaction heat recycling system in formaldehyde production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |