CN108325478A - A kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier - Google Patents
A kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier Download PDFInfo
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- CN108325478A CN108325478A CN201810145773.7A CN201810145773A CN108325478A CN 108325478 A CN108325478 A CN 108325478A CN 201810145773 A CN201810145773 A CN 201810145773A CN 108325478 A CN108325478 A CN 108325478A
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- 239000007788 liquid Substances 0.000 title claims abstract description 79
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 59
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 45
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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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
-
- 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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/085—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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/087—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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of falling film reactors of the hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, the top of reactor body is equipped with inlet tube, the bottom of reactor body is equipped with air inlet pipe, the top of reactor body is equipped with gas vent, the lower part of reactor body is equipped with drainage hole, in reactor body liquid distribution trough is equipped in the lower section of inlet tube, it is equipped with gas distributor in the top of air inlet pipe, the liquid distribution trough is bowl, bowl is fixedly connected by cantilever with reactor body inner wall, and there are gaps between the bowl outer wall and reactor body inner wall, reactor body inner wall is coated with catalyst for hydrogenation, reactor body outer wall is equipped with insulation jacket.Present invention inner wall coated with catalyst compared with conventional tank reactor is all to provide the region of hydrogenation reaction, improves reaction efficiency, the reaction time is reduced, to improve economy.
Description
Technical field
The invention belongs to hydrogen storage technology fields, and in particular to a kind of falling liquid film of hydrogenation reaction suitable for liquid hydrogen storage carrier
Reactor.
Background technology
Hydrogen Energy is clean secondary energy sources.In recent years, as Hydrogen Energy application technology develops gradually maturation, and whole world reply
The development of the lasting increase of climate change pressure, Hydrogen Energy industry is concerned in countries in the world, the prosperities such as the U.S., Germany, Japan
It is national in succession to promote development Hydrogen Energy industry to national energy strategic height.The National Development and Reform Commission, country in 2016
The publication of the joints such as Bureau of Energy《Energy technology revolution innovates action plan (2016-the year two thousand thirty)》(hair changes the energy [2016] 513
Number) energy technology revolution emphasis innovation course of action figure is proposed, 15 specific tasks are deployed, " Hydrogen Energy and fuel cell skill
Art is innovated " it is among them, indicate that Hydrogen Energy industry has been included into China national energy strategy.
Hydrogen Energy is in itself and there is no the competitive relations of same electric power, fossil fuel.On the contrary, the development of Hydrogen Energy can be abundant
Using the existing world-class energy supply infrastructure (power generation, power transmission and distribution, oil and natural gas pipe network) of China, transported with traffic
Defeated and energy storage is core market, the sustainable energy for pushing Chinese energy market to be dominated to supply in a distributed manner and new energy
Pattern is converted.
It is both domestic and external practice have shown that, Hydrogen Energy can be widely applied to fuel-cell vehicle, power generation, energy storage, can also mix natural
Gas is for industry and domestic gas.Hydrogen Energy as clean secondary energy sources have can scale storage characteristic, extensive use
Can partial alternative oil and natural gas, become the important component of energy-consuming, to reply climate change and ensure the energy supply
It should wait safely with certain supporting role.The advantage and characteristic for making full use of Hydrogen Energy, it is more than needed in Wind Power In China, photoelectricity, water power
Or abandon wind, abandon light, abandon the more area of water and city and area that urban distribution network peak, paddy period electric load differ greatly,
Hydrogen source is obtained using water electrolysis hydrogen production, according to the Economic Development Status of each department and industrial and agricultural products and living standards of the people etc.
Factor, the pattern for taking electricity-hydrogen-electricity, electricity-hydrogen-use or both to mix, consumption and storage electric power more than needed or crest segment electric power, help
In " bottleneck " of the structural surplus electricity of neutralizing power industry.
The technical research personnel of this field have carried out considerable research to hydrogenation reactor, and work out many kinds
The hydrogenation reactor of class, but the existing hydrogenation reactor used is mostly batch reactor, cannot achieve consecutive production,
Device amplification is not easy, and mass-and heat-transfer is ineffective, limits its application range.
Invention content
Present invention aims to overcome that the shortcomings that prior art with it is insufficient, provide a kind of suitable for liquid hydrogen storage carrier
The advantages that falling film reactor of hydrogenation reaction has continuous production, and pressure drop is small, no axial backmixing.
To achieve the above object, the technical solution adopted by the present invention is as follows：
A kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, reactor sheet
The top of body is equipped with inlet tube, and the bottom of reactor body is equipped with air inlet pipe, and the top of reactor body is equipped with gas vent, reaction
The lower part of device ontology is equipped with drainage hole, and reactor body is interior to be equipped with liquid distribution trough, in the upper of air inlet pipe in the lower section of inlet tube
Side is equipped with gas distributor, and the liquid distribution trough is bowl, and bowl is solid by cantilever and reactor body inner wall
Fixed connection, and there are gap between the bowl outer wall and reactor body inner wall, reactor body inner wall, which is coated with, to be added
Hydrogen catalysts, reactor body outer wall are equipped with insulation jacket.
The action principle of the present invention：Hydrogen storage carrier is by inlet tube input reactor ontology, hydrogen storage carrier fills liquid point
After cloth device, via the gap between liquid distribution trough and reactor body inner wall formed under gravity liquid film to flow down
Dynamic, gas is evenly dispersed in hydrogenation reactor ontology through gas distributor by air inlet pipe input reactor ontology, in air pressure
Under the action of flow up, hydrogenation reaction is exothermic reaction, and insulation jacket is hydrogenation reaction heat preservation, and hydrogen storage carrier is in specified reaction
At a temperature of hydrogenation reaction occur under the catalyst coat effect of inner wall with the hydrogen in gas become hydrogen source material, it is completely anti-
The liquid answered is discharged to by the drainage hole of reactor body outside reactor body, and the gas not reacted completely passes through reactor body
Row of exhausting-gas hole to reactor body outside.
It is hydrogen, hydrogen storage carrier and catalyst gas that falling film reactor of the present invention, which has great response area, hydrogenation reaction,
Liquid solid phase reaction needs larger response area, and the inner wall of catalyst is coated with compared with conventional tank reactor and is all
The region of hydrogenation reaction is provided, reaction efficiency is improved, the reaction time is reduced, to improve economy；And falling liquid film of the present invention is anti-
The downward liquid flow of device, gas is answered to flow up, it is axial to improve the purity of product without air-teturning mixed phenomenon, reduce rear end separation
Cost.
As an improvement of the present invention, the gas distributor is enclosed globe shade, and enclosed globe shade is fixed on the inner end of air inlet pipe,
Multiple air admission holes are provided on enclosed globe shade.
As a kind of improvement of the present invention, the lower part of the reactor body is equipped with fluid collection device, fluid collection device
It is connected with reactor body drainage hole, fluid collection device is equipped with drain pipe.
Further, the fluid collection device is the toroidal container for being fixed on reactor body lower external, and annular is held
Device is equipped with drain pipe, and the lower part of the reactor body is along the circumferential direction equipped with multiple drainage holes.
As a kind of improvement of the present invention, the top of the reactor body is equipped with gas collector, gas collector
It is connected with reactor body gas vent, gas collector is equipped with exhaust pipe.
Further, the gas collector is the toroidal container for being fixed on reactor body lower external, and annular is held
Device is equipped with exhaust pipe, and the top of the reactor body is along the circumferential direction equipped with multiple gas vents.
As a kind of improvement of the present invention, inwardly projecting cofferdam is equipped at gas vent surrounding in the reactor body.
As a kind of improvement of the present invention, liquid is equipped between liquid distribution trough and gas distributor in the reactor body
Body redistributor.
Further, the liquid re-distributor quantity is several, several liquid re-distributors are uniform from top to bottom
Distribution.
Further, the liquid re-distributor is conical ring, and downward, conical ring outer wall passes through outstanding the conical ring big end
Arm is fixedly connected with reactor body inner wall, and there are gaps with reactor body inner wall for conical ring outer wall.
Compared with prior art, the present invention has the following advantages：
1, it is hydrogen, hydrogen storage carrier and catalyst that falling film reactor of the present invention, which has great response area, hydrogenation reaction,
Gas-liquid-solid phase reaction needs larger response area, and the inner wall of catalyst is coated with all compared with conventional tank reactor
It is to provide the region of hydrogenation reaction, improves reaction efficiency, the reaction time is reduced, to improve economy.
2, the downward liquid flow of falling film reactor of the present invention, gas flow up, axial without air-teturning mixed phenomenon, improve production
The purity of object reduces rear end separation costs.
3, falling film reactor of the invention is provided with fluid collection device and gas collector, in the mistake of drain and exhaust
Two ring system cavitys provide cushioning effect in journey, reduce fluid local pressure in flow process it is excessive and caused by fluid
The phenomenon that being unevenly distributed.
4, falling film reactor of the present invention is without agitating equipment, because hydrogenation reaction is reacted for volume-diminished, the higher reaction effect of pressure
Fruit is better, and using agitating equipment such as agitating paddle, while with the presence of hydrogen in system, sealing difficulty is quite big, and falling film reactor is
Reach mass-and heat-transfer by the gravity flowing of liquid itself, be not necessarily to agitating equipment, leakproofness has sizable guarantee.
5, several liquid re-distributors, because liquid is when flowing downward, same stepping are set in the middle part of falling film reactor of the present invention
Row hydrogenation reaction can have the phenomenon that liquid film is unevenly distributed, by liquid re-distributor by liquid unevenly distributed again with
Uniform form of liquid film flows down, and improves reaction efficiency, meanwhile, the addition of liquid re-distributor can be played to a certain extent
The effect of fluid cushion can be stored in ring system is formed with inner wall three to adapt to changeable operating mode when under a large amount of liquid flow
It stores in angular ring system, then passes slowly the gap of bottom and flow down, to improve the utilization ratio of hydrogen storage carrier.
6, falling film reactor of the present invention uses heat carrier jacket for heat exchange mode, because hydrogenation reaction is exothermic reaction, therefore chuck
Effect be not only to maintain the temperature of reaction system, while partial reaction heat can also be taken out of, caused by preventing system temperature runaway
The problems such as catalyst carbon deposition inactivates, hydrogen storage carrier coking.
Description of the drawings
Fig. 1 is the schematic diagram of the falling film reactor for the hydrogenation reaction that the present invention is suitable for liquid hydrogen storage carrier.
Specific implementation mode
The invention will be further described with reference to the accompanying drawings and examples.It is understood that tool described herein
Body embodiment is used only for explaining the present invention rather than limitation of the invention.It also should be noted that for the ease of retouching
It states, only some but not all contents related to the present invention are shown in the drawings.
Embodiment
Referring to FIG. 1, a kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body
1, the top of reactor body 1 is equipped with inlet tube 11, and the bottom of reactor body 1 is equipped with air inlet pipe 12, reactor body 1 it is upper
Portion is equipped with gas vent 13, and the lower part of reactor body 1 is equipped with drainage hole 14, is set in the lower section of inlet tube 11 in reactor body 1
There is liquid distribution trough 2, be equipped with gas distributor 3 in the top of air inlet pipe 12；
The liquid distribution trough 2 is bowl 21, and bowl 21 is fixed by cantilever 22 and 1 inner wall of reactor body
Connection, specifically, the cantilever 22 are steel bar, steel bar one end is weldingly fixed on 1 inner wall of reactor body, the other end with it is bowl-shape
Container 21 is welded and fixed, and keeps bowl holding horizontal；
And there are gaps 23,1 inner wall of reactor body to apply between 21 outer wall of bowl and 1 inner wall of reactor body
It is covered with catalyst for hydrogenation, 1 outer wall of reactor body is equipped with insulation jacket 4.
The action principle of the present invention：Hydrogen storage carrier is by inlet tube input reactor ontology, hydrogen storage carrier fills liquid point
After cloth device, via the gap between liquid distribution trough and reactor body inner wall formed under gravity liquid film to flow down
Dynamic, gas is evenly dispersed in hydrogenation reactor ontology through gas distributor by air inlet pipe input reactor ontology, in air pressure
Under the action of flow up, hydrogenation reaction is exothermic reaction, and insulation jacket is hydrogenation reaction heat preservation, and hydrogen storage carrier is in specified reaction
At a temperature of hydrogenation reaction occur under the catalyst coat effect of inner wall with the hydrogen in gas become hydrogen source material, it is completely anti-
The liquid answered is discharged to by the drainage hole of reactor body outside reactor body, and the gas not reacted completely passes through reactor body
Row of exhausting-gas hole to reactor body outside.
It is hydrogen, hydrogen storage carrier and catalyst gas that falling film reactor of the present invention, which has great response area, hydrogenation reaction,
Liquid solid phase reaction needs larger response area, and the inner wall of catalyst is coated with compared with conventional tank reactor and is all
The region of hydrogenation reaction is provided, reaction efficiency is improved, the reaction time is reduced, to improve economy；And falling liquid film of the present invention is anti-
The downward liquid flow of device, gas is answered to flow up, it is axial to improve the purity of product without air-teturning mixed phenomenon, reduce rear end separation
Cost.In addition, because hydrogenation reaction is volume-diminished reaction, the higher reaction effect of pressure is better, using dynamic equipment such as agitating paddle, together
When system in the presence of hydrogen, sealing difficulty is quite big, and falling film reactor is to reach mass transfer by the gravity flowing of liquid itself
Heat transfer, without dynamic equipment, leakproofness has sizable guarantee；And heat carrier jacket for heat exchange mode is used, because of hydrogenation reaction
For exothermic reaction, therefore the effect of heat carrier is not only to maintain the temperature of reaction system, while can also take partial reaction heat out of, prevents
The problems such as only catalyst carbon deposition inactivates caused by system temperature runaway, hydrogen storage carrier coking.
The catalyst coat is that one layer of AlOOH colloidal sol is first coated in catalyst reaction wall, and one layer is generated by calcining
γ-Al2O3Coating, be then coated on this coating again one layer containing precious metals pt, Rh, Ru, Pd and non-noble metal Ni, Co,
Mg, Ca, Fe be one such or a variety of salts are as presoma, by calcine, restore to obtain precious metals pt, Rh, Ru, Pd and
Non-noble metal Ni, Co, Mg, Ca, Fe one of which or multicomponent catalyst,
In the present embodiment, the gas distributor 3 is enclosed globe shade 31, and enclosed globe shade 31 is fixed on the inner end of air inlet pipe 12,
Multiple air admission holes 32 are provided on enclosed globe shade 31.Using the enclosed globe shade for being provided with multiple air admission holes as gas distributor, will enter anti-
It answers the gas in device to redistribute, enables gas even into in reactor.
In the present embodiment, the lower part of the reactor body 1 is equipped with fluid collection device 7, fluid collection device 7 with it is anti-
1 drainage hole 14 of device ontology is answered to be connected, fluid collection device 7 is equipped with drain pipe 71.It is provided with fluid collection device, in drain
Cushioning effect is provided in the process, reduce liquid local pressure in flow process it is excessive and caused by liquid distribution is uneven shows
As.Specifically, the fluid collection device 7 is the toroidal container for being fixed on 1 lower external of reactor body, and toroidal container is equipped with
The lower part of drain pipe 71, the reactor body 1 is along the circumferential direction equipped with multiple drainage holes 14.It sets fluid collection device to
The structure of toroidal container can increase and collect area, more efficient collection liquid, and can be in reactor body lower part surrounding
Equipped with drainage hole, it can so that liquid flow is dynamic more uniformly.
In the present embodiment, the top of the reactor body 1 is equipped with gas collector 6, gas collector 6 with it is anti-
1 gas vent 13 of device ontology is answered to be connected, gas collector 6 is equipped with exhaust pipe 61.It is provided with gas collector, is being vented
Cushioning effect is provided in the process, reduce gas local pressure in flow process it is excessive and caused by showing of being unevenly distributed of gas
As.Specifically, the gas collector 6 is the toroidal container for being fixed on 1 lower external of reactor body, and toroidal container is equipped with
The top of exhaust pipe 61, the reactor body 1 is along the circumferential direction equipped with multiple gas vents 13.It sets gas collector to
The structure of toroidal container can increase and collect area, more efficient collection gas, and can be in reactor body top surrounding
Equipped with gas vent, it can so that gas stream is dynamic more uniformly.On the basis of the above, in gas vent 13 in the reactor body 1
Inwardly projecting cofferdam 62 is equipped at surrounding, specifically, the cofferdam 62 is the casing for being fixed on 13 outer rim of gas vent, equipped with enclosing
Weir can prevent the hydrogen storage carrier under overhead stream from flowing into gas collector.
In one embodiment of the invention, in the reactor body 1 liquid distribution trough 2 and gas distributor 3 it
Between be equipped with liquid re-distributor 5.It is synchronous to carry out hydrogenation reaction because liquid is when flowing downward, there can be liquid film and be unevenly distributed
Phenomenon is flowed down liquid unevenly distributed by liquid re-distributor with uniform form of liquid film again, improves reaction effect
Rate, meanwhile, the addition of liquid re-distributor can play the role of fluid cushion to a certain extent, to adapt to changeable work
Condition.Further, 5 quantity of the liquid re-distributor is several, several liquid re-distributors 5 from top to bottom uniformly divide
Cloth.
Specifically, the liquid re-distributor 5 be conical ring 51,51 big end of the conical ring downward, 51 outer wall of conical ring
It is fixedly connected with 1 inner wall of reactor body by cantilever 52, wherein the cantilever 51 is steel bar, and steel bar one end is weldingly fixed on
On 1 inner wall of reactor body, the other end and conical ring 51 be welded and fixed, and 51 outer wall of conical ring is stayed with 1 inner wall of reactor body
There is gap.It can be stored in the triangle ring system that conical ring is formed with reactor body inner wall and store when under a large amount of liquid flow
Get off, then pass slowly the gap of bottom and flow down, to improve the utilization ratio of hydrogen storage carrier.
In falling film reactor of the present invention, the gas is the gaseous mixture of pure hydrogen or hydrogen and other inert gases；
In falling film reactor of the present invention, the hydrogen storage carrier is that unsaturated arene compound and/or heterocycle are unsaturated
Compound is one such or a variety of with solvent mixture, wherein mUnsaturated arene compound and/or heterocycle unsaturated compoundWith mSolventProportional region
For 0.03-0.97；
In falling film reactor of the present invention, the unsaturation arene compound is selected from benzene, toluene, ethylbenzene, propyl benzene, isopropyl
Benzene, ortho-xylene, paraxylene, meta-xylene, styrene, naphthalene, anthracene, phenanthrene, phenol, aniline and its derivatives；The heterocycle is not
Saturated compounds is being selected from carbazole, indoles, N- methyl carbazoles, N- ethyl carbazoles, N- n-propyls carbazole, N- isopropylcarbazoles, N- just
Butyl carbazole, N- methyl indols, N- ethylindoles, pyrazine, furans, pyrroles, thiazole, pyridine, penta pyrazine of ring, benzothiazole and its
Derivative；The solvent be selected from methanol, ethyl alcohol, isopropanol, ethylene glycol, normal propyl alcohol, n-butanol, ether, methyl ether, acetonitrile, formic acid,
Acetic acid, ethyl acetate, methyl acetate, Ethyl formate, n-butyl ether, isopropyl ether, dichloromethane, chloroform, tetrachloromethane, two chloroethenes
Alkane, n-hexane, hexamethylene, pentane, normal octane, carbon disulfide, petroleum ether are one such or a variety of.
The above embodiment is a preferred embodiment of the present invention, but embodiments of the present invention are not by above-described embodiment
Limitation, it is other it is any without departing from the spirit and principles of the present invention made by changes, modifications, substitutions, combinations, simplifications,
Equivalent substitute mode is should be, is included within the scope of the present invention.
Claims (10)
1. a kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, reactor body
Top be equipped with inlet tube, the bottom of reactor body is equipped with air inlet pipe, and the top of reactor body is equipped with gas vent, reactor
The lower part of ontology is equipped with drainage hole, it is characterised in that：In reactor body the lower section of inlet tube be equipped with liquid distribution trough, into
The top of tracheae is equipped with gas distributor, and the liquid distribution trough is bowl, and bowl passes through cantilever and reactor sheet
Internal wall is fixedly connected, and there are gap, reactor body inner walls between the bowl outer wall and reactor body inner wall
Coated with catalyst for hydrogenation, reactor body outer wall is equipped with insulation jacket.
2. the falling film reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, it is characterised in that：
The gas distributor is enclosed globe shade, and enclosed globe shade is fixed on the inner end of air inlet pipe, multiple air admission holes are provided on enclosed globe shade.
3. the falling film reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, it is characterised in that：
The lower part of the reactor body is equipped with fluid collection device, and fluid collection device is connected with reactor body drainage hole, liquid
Body collection device is equipped with drain pipe.
4. the falling film reactor of the hydrogenation reaction according to claim 3 suitable for liquid hydrogen storage carrier, it is characterised in that：
The fluid collection device is the toroidal container for being fixed on reactor body lower external, and toroidal container is equipped with drain pipe, described
The lower part of reactor body is along the circumferential direction equipped with multiple drainage holes.
5. the falling film reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, it is characterised in that：
The top of the reactor body is equipped with gas collector, and gas collector is connected with reactor body gas vent, gas
Body collection device is equipped with exhaust pipe.
6. the falling film reactor of the hydrogenation reaction according to claim 5 suitable for liquid hydrogen storage carrier, it is characterised in that：
The gas collector is the toroidal container for being fixed on reactor body lower external, and toroidal container is equipped with exhaust pipe, described
The top of reactor body is along the circumferential direction equipped with multiple gas vents.
7. the falling film reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, it is characterised in that：
Inwardly projecting cofferdam is equipped in the reactor body at gas vent surrounding.
8. the falling film reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, it is characterised in that：
Liquid re-distributor is equipped in the reactor body between liquid distribution trough and gas distributor.
9. the falling film reactor of the hydrogenation reaction according to claim 8 suitable for liquid hydrogen storage carrier, it is characterised in that：
The liquid re-distributor quantity is several, several liquid re-distributors are from top to bottom uniformly distributed.
10. the falling film reactor of the hydrogenation reaction according to claim 8 suitable for liquid hydrogen storage carrier, feature exist
In：The liquid re-distributor is conical ring, and downward, conical ring outer wall passes through cantilever and reactor body to the conical ring big end
Inner wall is fixedly connected, and there are gaps with reactor body inner wall for conical ring outer wall.
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| CN201810145773.7A CN108325478A (en) | 2018-02-12 | 2018-02-12 | A kind of falling film reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109316927A (en) * | 2018-11-09 | 2019-02-12 | 中国科学院过程工程研究所 | A kind of tapering type ozone uniform device and its arrangement in flue |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH414045A (en) * | 1963-06-20 | 1966-05-31 | Gulf Research Development Co | Hydrocracking process for liquid hydrocarbons |
| US4141690A (en) * | 1977-08-05 | 1979-02-27 | Uop Inc. | Catalytic reaction chamber for gravity-flowing catalyst particles |
| US5939031A (en) * | 1996-08-23 | 1999-08-17 | Exxon Research And Engineering Co. | Countercurrent reactor |
| DE69729942D1 (en) * | 1997-10-06 | 2004-08-26 | Indian Oil Corp Ltd | Process and device for fluid catalytic cleavage |
| US20050188619A1 (en) * | 2004-03-01 | 2005-09-01 | Thomas Rostrup-Nielsen | Process for cooling an exothermic reaction zone and reactor unit |
| US20050240058A1 (en) * | 2003-07-04 | 2005-10-27 | Nongyue Wang And Guangqiang Shi | Process for preparing 4-aminodiphenylamine |
| CN1872819A (en) * | 2005-05-31 | 2006-12-06 | 中国石油化工股份有限公司 | Counter flow typed selective method for adding hydrogen |
| WO2008145683A1 (en) * | 2007-06-01 | 2008-12-04 | Dsm Fine Chemicals Austria Nfg Gmbh & Co Kg | Tube bundle falling film microreactor for performing gas liquid reactions |
| CN203648502U (en) * | 2013-11-25 | 2014-06-18 | 南京国昌化工科技有限公司 | Uniform-temperature hydrogenation reactor |
| CN204208536U (en) * | 2014-10-23 | 2015-03-18 | 中国石油化工股份有限公司 | The hybrid system of hydrogen and hydrocarbon ils in a kind of up-flow reactor |
| CN206715895U (en) * | 2017-04-27 | 2017-12-08 | 天津奥展兴达化工技术有限公司 | Gas distributor and the reactor comprising the gas distributor |
| CN208145929U (en) * | 2018-02-12 | 2018-11-27 | 北京国能中林科技开发有限公司 | A kind of falling film reactor of the hydrogenation reaction suitable for liquid hydrogen storage carrier |
-
2018
- 2018-02-12 CN CN201810145773.7A patent/CN108325478A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH414045A (en) * | 1963-06-20 | 1966-05-31 | Gulf Research Development Co | Hydrocracking process for liquid hydrocarbons |
| US4141690A (en) * | 1977-08-05 | 1979-02-27 | Uop Inc. | Catalytic reaction chamber for gravity-flowing catalyst particles |
| US5939031A (en) * | 1996-08-23 | 1999-08-17 | Exxon Research And Engineering Co. | Countercurrent reactor |
| DE69729942D1 (en) * | 1997-10-06 | 2004-08-26 | Indian Oil Corp Ltd | Process and device for fluid catalytic cleavage |
| US20050240058A1 (en) * | 2003-07-04 | 2005-10-27 | Nongyue Wang And Guangqiang Shi | Process for preparing 4-aminodiphenylamine |
| US20050188619A1 (en) * | 2004-03-01 | 2005-09-01 | Thomas Rostrup-Nielsen | Process for cooling an exothermic reaction zone and reactor unit |
| CN1872819A (en) * | 2005-05-31 | 2006-12-06 | 中国石油化工股份有限公司 | Counter flow typed selective method for adding hydrogen |
| WO2008145683A1 (en) * | 2007-06-01 | 2008-12-04 | Dsm Fine Chemicals Austria Nfg Gmbh & Co Kg | Tube bundle falling film microreactor for performing gas liquid reactions |
| CN203648502U (en) * | 2013-11-25 | 2014-06-18 | 南京国昌化工科技有限公司 | Uniform-temperature hydrogenation reactor |
| CN204208536U (en) * | 2014-10-23 | 2015-03-18 | 中国石油化工股份有限公司 | The hybrid system of hydrogen and hydrocarbon ils in a kind of up-flow reactor |
| CN206715895U (en) * | 2017-04-27 | 2017-12-08 | 天津奥展兴达化工技术有限公司 | Gas distributor and the reactor comprising the gas distributor |
| CN208145929U (en) * | 2018-02-12 | 2018-11-27 | 北京国能中林科技开发有限公司 | A kind of falling film reactor of the hydrogenation reaction suitable for liquid hydrogen storage carrier |
Non-Patent Citations (1)
| Title |
|---|
| （美）耶蒂什·特·夏: "气液固反应器设计", 化学工业出版社, pages: 29 - 10 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109316927A (en) * | 2018-11-09 | 2019-02-12 | 中国科学院过程工程研究所 | A kind of tapering type ozone uniform device and its arrangement in flue |
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Effective date of registration: 20230323 Address after: Room 901-4, No. 9, Kehui 1st Street, Science City, Huangpu District, Guangzhou City, Guangdong Province, 510000 Applicant after: Guoneng Hydrogen Oil (Guangdong) Technology Co.,Ltd. Address before: 102199 room 1301, 13th floor, building 7, yard 15, Ronghua South Road, Beijing Economic and Technological Development Zone, Daxing District, Beijing Applicant before: BEIJING GUONENG ZHONGLIN SCI-TECHNOLOGY DEVELOPMENT CO.,LTD. |
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Application publication date: 20180727 |