CN206492484U - A kind of straight tube header coil pipe reactor of water route Natural Circulation - Google Patents
A kind of straight tube header coil pipe reactor of water route Natural Circulation Download PDFInfo
- Publication number
- CN206492484U CN206492484U CN201720089701.6U CN201720089701U CN206492484U CN 206492484 U CN206492484 U CN 206492484U CN 201720089701 U CN201720089701 U CN 201720089701U CN 206492484 U CN206492484 U CN 206492484U
- Authority
- CN
- China
- Prior art keywords
- pipe
- header
- straight tube
- inflator
- pressure
- 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 straight tube header coil pipe reactor of water route Natural Circulation, the heat-exchanging tube bundle includes outlet pipe, upper straight tube header, coiled pipe, lower straighttube header, branch pipe, endless tube and water inlet pipe, the outlet pipe is connected to the top of pressure-bearing shell, the upper straight tube header connects the import of outlet pipe and the outlet of coiled pipe respectively, axial direction distribution of the coiled pipe along pressure-bearing shell, the import for connecting the coiled pipe respectively of the lower straighttube header and the outlet of branch pipe, the water inlet pipe is connected to the bottom of pressure-bearing shell, the endless tube connects water inlet pipe and branch pipe respectively.The utility model uses coiled pipe for main heat-exchanging tube bundle, and coiled pipe tube bank thoroughly eliminates thermal stress on axially and radially；Ensure that gas flows radially across beds using outer inflator and interior inflator technology, gas flow direction is plumbness with water flow direction；Waterway circulating multiplying power is high；Loaded catalyst is more, moves heat energy power by force, be easy to maximization.
Description
Technical field
The utility model is related to a kind of chemical reactor, more particularly to a kind of water route Natural Circulation straight tube 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.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art there is provided a kind of straight tube 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
Pipe, upper straight tube header, coiled pipe, lower straighttube header, branch pipe, endless tube and water inlet pipe, the outlet pipe are connected to the top of pressure-bearing shell
Portion, the upper straight tube header connects the import of outlet pipe and the outlet of coiled pipe, axial direction of the coiled pipe along pressure-bearing shell point respectively
Cloth, the import for connecting the coiled pipe respectively of the lower straighttube header and the outlet of branch pipe, the water inlet pipe are connected to pressure-bearing shell
The bottom of body, the endless tube connects water inlet pipe and branch pipe respectively；The upper straight tube header is identical with lower straighttube header structure, respectively
Including the multiple connecting tubes radially angularly set along pressure-bearing shell, the connecting tube is vertically set on the horizontal stroke of the pressure-bearing shell
On section, one end connection coiled pipe of the connecting tube, the other end connects corresponding pipeline.
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；The flat cover is arranged on the top of straight tube header,
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 inflator and interior
In space between inflator, there is space, upper straight tube header and lower straighttube the header difference between the outer inflator and housing
The top and bottom of outer inflator are arranged on, the lower straighttube header is supported in support platform, it is the outlet pipe, flat cover, upper straight
Loading catalyst in the space that pipe header, outer inflator, coiled pipe, interior inflator, lower straighttube header, branch pipe, endless tube, water inlet pipe are formed.
The angle of the adjacent connecting tube is 45 °.Upper straight tube header and lower straighttube header uniformly can be distributed on coiled pipe
Turnover water.
A kind of method that hydrogenation reaction is carried out using described reactor.
The method of the hydrogenation reaction, 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, upper gas port enters reacting gas, catalyst bed is passed radially through by outer inflator
To interior inflator hydrogenation reaction occurs for layer；
(13) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe removes the heat after the hydrogenation reaction of catalyst inframe, gas
Then collected by interior inflator, then discharged through lower gas port and take away heat.
A kind of method that use reactor carries out oxonation.
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, and catalyst bed is passed radially through by interior inflator
To outer inflator oxonation occurs for layer；
(23) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe removes the heat of the oxonation of catalyst inframe, gas is 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 cloth tube angulation is at 10~80 °, coiled pipe and pressure-bearing shell
Angle between axial direction, coiled pipe using move axially (between two coiled pipes) or move radially (coiled pipe diameter become big or diminish) come
Thermal stress is eliminated, realizes that coiled pipe tube bank thoroughly eliminates thermal stress on axially and radially；It is true using outer inflator and interior inflator technology
Protect gas and flow radially across beds, bed resistance≤0.001MPa of oxonation, the bed resistance of hydrogenation reaction≤
0.005MPa；Coiled pipe is used for main heat-exchanging tube bundle, flat outside water-intake pipe in pipe, gas flow direction and water flow direction are vertical
Straight state；Use the waterway circulating between drum and coiled pipe tube bank to follow naturally, waterway circulating multiplying power is high；It is main to use coiled pipe
Heat-exchanging tube bundle combines with radial gas distributor technology, and loaded catalyst is more, it is strong to move heat energy power, while catalyst
All it can expose outside, reaction is abundant.
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 anti-
The security and stability of device is answered, heat exchanger plates in the easy leakage of shell and tube reactor in the prior art and plate-type reactor is prevented effectively from and holds
The defects such as easy leakage；
2nd, the technology combined using outer inflator and interior inflator ensures that gas flows radially across beds, effectively reduces carbonylation
Or hydrogenation reaction circulator power consumption, in oxonation ethylene glycol per ton can reduce circulator power consumption 300KW.h/t ethylene glycol with
On, ethylene glycol per ton can be reduced more than circulator power consumption 100KW.h/t ethylene glycol in hydrogenation 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
It is prompt；
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) and nitrous acid heating thermal decomposition phenomenon (carbonyl
Change reaction) occur, prevent security incident；
5th, gas Radial Flow, resistance are low, and loaded catalyst is more, it is strong to move heat energy power, meets glycol unit maximization
Need, the oxonation device or hydrogenation reactor one of 10~300,000 tons of ethylene glycol, carbonylation/hydrogenation plant are only one and are
Row, can make existing carbonylation/hydrogenation plant floor space reduce by more than 50%, construction investment reduction by more than 50%, operation operation
Expense reduction by more than 40%.
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.
Brief description of the drawings
Fig. 1 is that the utility model applies the structural representation in hydrogenation reaction；
Fig. 2 is that the utility model applies the structural representation in oxonation；
Fig. 3 is the structural representation of upper straight tube header.
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 includes outlet pipe 4, upper straight tube header 7, coiled pipe 11, lower straight
Pipe header 13, branch pipe 14, endless tube 15 and water inlet pipe 18, the outlet pipe 4 are connected to the top of pressure-bearing shell, the upper straight tube connection
Case 7 connects the import of outlet pipe 4 and the outlet of coiled pipe 11 respectively, axial direction distribution of the coiled pipe 11 along pressure-bearing shell, it is described under
The import for connecting the coiled pipe 11 respectively and the outlet of branch pipe 14 of straight tube header 13, the water inlet pipe 18 are connected to pressure-bearing shell
Bottom, the endless tube 15 connects water inlet pipe 18 and branch pipe 14 respectively, and pressure-bearing shell includes upper cover 5, housing 9, support platform
16th, low head 17；The upper cover 5 and housing 9 are connected by flange 8, and the support platform 16 is arranged on low head 17, institute
State the bottom that low head 17 is fixed on housing 9.Pressure-bearing shell is not involved in reaction, is primarily subjected to pressure, pyroreaction gas is not contacted
Body；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 described
End socket 17 is provided with lower gas port 20, water inlet 19 and catalyst self-unloading mouth 21；The water inlet pipe 18 is arranged in water inlet 19.
The catalyst framework includes flat cover 6, outer inflator 10, interior inflator 12；The flat cover 6 is arranged on straight tube header 7
Top, the outer inflator 10 is along the axially arranged of housing 9, and the interior inflator 12 is set in outer inflator 10, the coiled pipe 11
It is arranged in the space between outer inflator 10 and interior inflator 12, there is space between the outer inflator 10 and housing 9, it is described straight
Pipe header 7 and lower straighttube header 13 are separately positioned on the top and bottom of outer inflator 10, and the lower straighttube header 13 is supported on
Support on platform 16, the outlet pipe 4, flat cover 6, upper straight tube header 7, outer inflator 10, coiled pipe 11, interior inflator 12, lower straighttube header
13rd, loading catalyst in the space that branch pipe 14, endless tube 15, water inlet pipe 18 are formed.
As shown in figure 3, the upper straight tube header 7 is identical with the structure of lower straighttube header 13, respectively including along pressure-bearing shell footpath
To the multiple connecting tubes 22 angularly set, the angle of adjacent connecting tube 22 is 45 °.The connecting tube 22 is vertically set on described
On the cross section of pressure-bearing shell, one end connection coiled pipe of the connecting tube 22, the other end connects corresponding pipeline, upper straight tube header
The connection coiled pipe of connecting tube 22 on the outlet and the outlet of outlet pipe 4 of the connection coiled pipe 11 of connecting tube 22 on 7, lower straighttube header 13
11 import and the outlet of branch pipe 14.Upper straight tube header 7 and lower straighttube header 13 can uniformly be distributed the Inlet and outlet water on coiled pipe
Amount.
The method that the present embodiment carries out hydrogenation reaction using described 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 occurs for agent bed；
(13) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe 11 removes the heat after the hydrogenation reaction of catalyst inframe, gas
Body is then collected by interior inflator 12, is then discharged through lower gas port 20 and is taken away heat.
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 is released heat and urged by water absorption removal in coiled pipe 11
Agent bed heat, and by-product 1.0~2.5MPa saturated vapors.
Embodiment 2
As shown in Fig. 2 the method that the present embodiment carries out oxonation using 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 20 enters reacting gas, pass radially through and urge by interior inflator 12
To outer inflator 10 oxonation occurs for agent bed；
(23) after reacting, the aqueous phase changeable heat-absorbing in coiled pipe 11 removes the heat of the oxonation of catalyst inframe, gas
Then collected by outer inflator 10, then discharged through upper gas port 3 and take 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.
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 straight tube 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, upper straight tube header, coiled pipe, lower straighttube header, branch pipe, endless tube and water inlet pipe, the outlet pipe are connected to pressure-bearing shell
Top, the upper straight tube header connects the import of outlet pipe and the outlet of coiled pipe, axial direction of the coiled pipe along pressure-bearing shell respectively
Distribution, the import for connecting the coiled pipe respectively of the lower straighttube header and the outlet of branch pipe, the water inlet pipe are connected to pressure-bearing
The bottom of housing, the endless tube connects water inlet pipe and branch pipe respectively；The upper straight tube header is identical with lower straighttube header structure, point
The multiple connecting tubes that Bao Kuo angularly do not set radially along pressure-bearing shell, the connecting tube is vertically set on the pressure-bearing shell
On cross section, one end connection coiled pipe of the connecting tube, the other end connects corresponding pipeline.
2. a kind of straight tube 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 straight tube 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 straight tube 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 straight tube header coil pipe reactor of water route Natural Circulation according to claim 2, it is characterised in that institute
Stating catalyst framework includes flat cover, outer inflator, interior inflator；The flat cover is arranged on the top of straight tube header, the outer inflator
Along the axially arranged of housing, the interior inflator is set in outer inflator, and the coiled pipe is arranged between outer inflator and interior inflator
In space, there is space, upper the straight tube header and lower straighttube header are separately positioned on outer gas between the outer inflator and housing
The top and bottom of cylinder, the lower straighttube header is supported in support platform, the outlet pipe, flat cover, upper straight tube header, outer gas
Loading catalyst in the space that cylinder, coiled pipe, interior inflator, lower straighttube header, branch pipe, endless tube, water inlet pipe are formed.
6. a kind of straight tube header coil pipe reactor of water route Natural Circulation according to claim 1, it is characterised in that institute
The angle for stating adjacent connecting tube is 45 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089701.6U CN206492484U (en) | 2017-01-23 | 2017-01-23 | A kind of straight tube header coil pipe reactor of water route Natural Circulation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720089701.6U CN206492484U (en) | 2017-01-23 | 2017-01-23 | A kind of straight tube header coil pipe reactor of water route Natural Circulation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206492484U true CN206492484U (en) | 2017-09-15 |
Family
ID=59803725
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720089701.6U Active CN206492484U (en) | 2017-01-23 | 2017-01-23 | A kind of straight tube header coil pipe reactor of water route Natural Circulation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206492484U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582455A (en) * | 2017-01-23 | 2017-04-26 | 南京敦先化工科技有限公司 | Straight pipe header coil pipe type reactor for waterway natural circulation |
| CN110739090A (en) * | 2019-10-14 | 2020-01-31 | 哈尔滨工程大学 | passive waste heat removal system of heat pipe stack cooled by wall surface of pressure container |
-
2017
- 2017-01-23 CN CN201720089701.6U patent/CN206492484U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582455A (en) * | 2017-01-23 | 2017-04-26 | 南京敦先化工科技有限公司 | Straight pipe header coil pipe type reactor for waterway natural circulation |
| CN110739090A (en) * | 2019-10-14 | 2020-01-31 | 哈尔滨工程大学 | passive waste heat removal system of heat pipe stack cooled by wall surface of pressure container |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| 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 | |
| WO2016045585A1 (en) | Large reactor and device and process thereof | |
| CN106582455A (en) | Straight pipe header coil pipe type reactor for waterway natural circulation | |
| CN106732311A (en) | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation | |
| CN105457563A (en) | Isothermal shift reactor with built-in tube bundle | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN102895922B (en) | Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester | |
| CN102160981B (en) | Catalytic reaction equipment | |
| CN206492484U (en) | A kind of straight tube header coil pipe reactor of water route Natural Circulation | |
| CN104368279A (en) | Radial constant-temperature reactor by using water to transfer heat | |
| CN104437266B (en) | Phase change heat absorption temperature control reactor | |
| CN203075923U (en) | Axial-radial constant-temperature conversion reactor | |
| CN202516536U (en) | Shift-converter with built-in cold wall | |
| CN206500146U (en) | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation | |
| CN104368282B (en) | The water bed reactor of beam tube type | |
| CN103585933B (en) | A kind of corrugated plate dst samming hydrogenation reactor | |
| CN205973791U (en) | Hydrogen peroxide solution production hydrogenation uses novel fixed bed | |
| CN208742509U (en) | A kind of water-cooled snakelike heat exchange tube axial flow reactor | |
| CN201701922U (en) | Catalytic reaction equipment | |
| CN202460592U (en) | Temperature stress resistant heat transfer reactor and composite device thereof | |
| CN204051637U (en) | A kind of built-in tube bank isothermal shift-converter | |
| CN216538373U (en) | Final stage water transfer heat bed layer ammonia synthesis reactor | |
| CN108654522A (en) | A kind of coil jacket formula axial flow reactor | |
| CN102886231A (en) | Fully-radial isothermal CO (carbon monoxide) conversion furnace |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |