CN108704600A - A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier - Google Patents
A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier Download PDFInfo
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- CN108704600A CN108704600A CN201810827366.4A CN201810827366A CN108704600A CN 108704600 A CN108704600 A CN 108704600A CN 201810827366 A CN201810827366 A CN 201810827366A CN 108704600 A CN108704600 A CN 108704600A
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- reactor body
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- reactor
- hydrogen storage
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 67
- 239000001257 hydrogen Substances 0.000 title claims abstract description 67
- 239000007788 liquid Substances 0.000 title claims abstract description 67
- 238000003860 storage Methods 0.000 title claims abstract description 38
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 27
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 230000000630 rising effect Effects 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims abstract description 17
- 230000007423 decrease Effects 0.000 claims abstract description 9
- 238000007789 sealing Methods 0.000 claims abstract description 7
- 238000004321 preservation Methods 0.000 claims abstract description 6
- 230000002093 peripheral effect Effects 0.000 claims abstract description 4
- 230000008676 import Effects 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 17
- 230000000694 effects Effects 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 230000004044 response Effects 0.000 description 6
- 230000009471 action Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 150000002431 hydrogen Chemical group 0.000 description 3
- 238000003746 solid phase reaction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000000576 coating method Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 239000010970 precious metal Substances 0.000 description 2
- 229910052703 rhodium Inorganic materials 0.000 description 2
- 229910052707 ruthenium Inorganic materials 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 229910002706 AlOOH Inorganic materials 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000001535 kindling effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000005622 photoelectricity Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910003158 γ-Al2O3 Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
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 Airlift circulating reactors of the hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, the heating jacket of the promising hydrogenation reaction heat preservation of reactor body peripheral hardware, it is equipped with exhaust pipe at the top of reactor body, the pipeline being located at immediately below exhaust pipe is equipped in reactor body, pipeline is suspended vacantly in reactor body, liquid decline passway is formed in pipeline, gap between pipeline and reactor body inner wall forms gas-liquid mixed rising passway, the side wall of pipeline is equipped with deflector hole, diversion pipe is connected at deflector hole, the free end of diversion pipe is extend out to outside reactor body, it is each coated with catalyst coat on reactor body inner wall and pipeline outer wall；Reactor body bottom is equipped with feeding device, and reactor body bottom is arranged right below inlet duct gas-liquid mixed rising passway.The present invention improves reaction efficiency, the reaction time is reduced, to improve economy；The leakproofness of the present invention has sizable guarantee, reduces sealing cost.
Description
Technical field
The invention belongs to hydrogen storage technology fields, and in particular to a kind of gas lift of hydrogenation reaction suitable for liquid hydrogen storage carrier
Formula circulation flow reactor.
Background technology
Hydrogen is the gas of colorless and odorless, and ignition energy is only 0.019mJ, belongs to Class A inflammable gas, is mixed with air
Explosive mixture, explosion limit ranging from 4.1%~74.1% can be formed.Hydrogen diffusivity is strong, easily leaks and is not easy to be noticeable；
Density is low, is easy to gather at the top of equipment, container and construction of structures, meets kindling material, heat source and burning, explosion occurs.
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.
Although hydrogen has extensive energy substitution foreground, since hydrogen density is very low, when hydrogen is open to one
It after spatial leaks, can spread rapidly, and earthward be dripped after Fuel Petroleum leakage, can also penetrate into gap, burning is rapid, fierce,
Therefore hydrogen reaction requires higher-security and heat transfer efficiency to hydrogenation reactor.And it is anti-to work out number of types of plus hydrogen
Device is answered, but the existing hydrogenation reactor used is mostly batch reactor, cannot achieve consecutive production, device amplifies not
Easily, 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 Airlift circulating reactor of hydrogenation reaction has continuous production, and gas residence time is long, is reached by gas itself agitation liquid
The advantages that enhancing mass and heat transfer.
To achieve the above object, the technical solution adopted by the present invention is as follows：
A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, instead
The heating jacket of the promising hydrogenation reaction heat preservation of device ontology peripheral hardware is answered, exhaust pipe, the reactor are equipped at the top of reactor body
The pipeline being located at immediately below exhaust pipe is equipped in ontology, the pipeline is suspended vacantly in reactor body, shape in the pipeline
At liquid decline passway, the gap between the pipeline and reactor body inner wall forms gas-liquid mixed rising passway, the pipe
The side wall in road is equipped with deflector hole, is connected with diversion pipe at deflector hole, the free end of diversion pipe is extend out to outside reactor body, institute
It states and is each coated with catalyst coat on reactor body inner wall and pipeline outer wall；The reactor body bottom is filled equipped with feed liquor
It sets, the reactor body bottom is in the inlet duct that is arranged right below of gas-liquid mixed rising passway, the liquid hydrogen storage carrier
It is entered in reactor body from feeding device, hydrogen is injected into reactor body from inlet duct and by liquid hydrogen storage carrier
It is brought into gas-liquid mixed rising passway.
The action principle of the present invention：Liquid hydrogen storage carrier is entered the bottom of reactor body by feeding device, and hydrogen passes through
Inlet duct injects reactor body, and liquid hydrogen storage carrier is brought into gas-liquid mixed rising passway, rises in gas-liquid mixed
Hydrogen gas bubbles are broken into minute bubbles and are uniformly mixed with hydrogen storage carrier in channel, liquid hydrogen storage carrier under specified reaction temperature with gas
Under the effect of the catalyst coat of reactor body inner wall and pipeline outer wall hydrogenation reaction, which occurs, for the hydrogen in body becomes hydrogen source material
Material, gas-liquid mixture flow up under the impetus of gas；Wherein, hydrogenation reaction is exothermic reaction, and heating jacket is to add
Hydrogen reaction heat preservation, gas-liquid mixture reach the gas-liquid separation region on reactor body top via rising passway, and hydrogen gas bubbles are de-
Reactor body is discharged by exhaust pipe from hydrogen source material, partially liq is under the driving force double action of gravity and hydrogen in liquid
It drops to reactor body bottom in decline passway to mix with new liquid hydrogen storage carrier, partially liq passes through the drain in pipeline
Reactor body is discharged in pipe.
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, compared with conventional tank reactor, outside reactor body inner wall and pipeline
Wall is each coated with catalyst, is all to provide the region of hydrogenation reaction, improves reaction efficiency, the reaction time is reduced, to improve warp
Ji property；Without equipment is moved in reactor body of the present invention, because hydrogenation reaction is reacted for volume-diminished, the higher reaction effect of pressure is more
Good, leakproofness has sizable guarantee, reduces sealing cost；The present invention uses heating jacket heat exchange mode, because of hydrogenation reaction
For exothermic reaction, therefore the effect of heating jacket is not only to maintain the temperature of reaction system, while can also take partial reaction heat out of,
The problems such as catalyst carbon deposition inactivates caused by preventing system temperature runaway, hydrogen storage carrier coking.
As an improvement of the present invention, the feeding device includes inlet tube, and inlet tube inserting is fixed on reactor sheet
The upper orifice of body bottom and the underface for being located at liquid decline passway, inlet tube is equipped with sealing cover, the surrounding of inlet tube upper side wall
Uniformly it is provided with inlet opening.
As an improvement of the present invention, the inlet duct includes air inlet pipe and ring pipe, and air inlet pipe is fixed on reaction
Device body bottom portion, ring pipe is fixed on air inlet pipe inner end, and ring pipe is connected with air inlet pipe inner end, ring pipe roof upper edge circle
Circumferential direction is provided with multiple ventholes, and the venthole is located at the underface of gas-liquid mixed rising passway.
Further, the heating jacket is equipped with heat carrier import and heating medium outlet, and the heat carrier import is located at
The top of heating jacket, the heating medium outlet are located at the lower part of heating jacket.
Compared with prior art, the present invention has the following advantages：
1, it is hydrogen, liquid hydrogen storage carrier and catalyst that reactor of the present invention, which has great response area, hydrogenation reaction,
Gas-liquid-solid phase reaction needs larger response area, compared with conventional tank reactor, reactor body inner wall and pipeline
Outer wall is each coated with catalyst, is all to provide the region of hydrogenation reaction, improves reaction efficiency, the reaction time is reduced, to improve
Economy；
2, without equipment is moved in reactor body of the present invention, because hydrogenation reaction is reacted for volume-diminished, the higher reaction effect of pressure
Fruit is better, and leakproofness has sizable guarantee, reduces sealing cost；
3, the present invention uses heating jacket heat exchange mode, and because hydrogenation reaction is exothermic reaction, therefore the effect of heating jacket is not
It is only to maintain the temperature of reaction system, while partial reaction heat can also be taken out of, catalyst accumulates caused by preventing system temperature runaway
The problems such as carbon inactivates, hydrogen storage carrier coking.
Description of the drawings
Fig. 1 is the schematic diagram of the Airlift circulating reactor for the hydrogenation reaction that the present invention is suitable for liquid hydrogen storage carrier；
Fig. 2 is the Airlift circulating reactor inlet duct annular for the hydrogenation reaction that the present invention is suitable for liquid hydrogen storage carrier
The schematic diagram of pipe.
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
It please refers to Fig.1 to Fig. 2, a kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, wraps
Include reactor body 10, the heating jacket 20 of the promising hydrogenation reaction heat preservation of 10 peripheral hardware of reactor body, 10 top of reactor body
Be equipped with exhaust pipe 11；
The pipeline 30 being located at immediately below exhaust pipe 11 is equipped in the reactor body 10, the pipeline 30 is suspended vacantly
In reactor body 10, form liquid decline passway 70 in the pipeline 30, the pipeline 30 and 10 inner wall of reactor body it
Between gap form gas-liquid mixed rising passway 60, the side wall of the pipeline 30 is equipped with deflector hole 31, is connected at deflector hole 31
There are diversion pipe 32, the free end of diversion pipe 32 to extend out to outside reactor body 10,10 inner wall of the reactor body and pipeline 30
Catalyst coat is each coated on outer wall；
10 bottom of the reactor body is equipped with feeding device 40, and 10 bottom of the reactor body rises in gas-liquid mixed
Channel 60 is arranged right below inlet duct 50, and the liquid hydrogen storage carrier enters to reactor body 10 from feeding device 40
Interior, hydrogen is injected into reactor body 10 from inlet duct 50 and liquid hydrogen storage carrier is brought into gas-liquid mixed rising passway
60。
The action principle of the present invention：Liquid hydrogen storage carrier is entered the bottom of reactor body by feeding device, and hydrogen passes through
Inlet duct injects reactor body, and liquid hydrogen storage carrier is brought into gas-liquid mixed rising passway, rises in gas-liquid mixed
Hydrogen gas bubbles are broken into minute bubbles and are uniformly mixed with hydrogen storage carrier in channel, liquid hydrogen storage carrier under specified reaction temperature with gas
Under the effect of the catalyst coat of reactor body inner wall and pipeline outer wall hydrogenation reaction, which occurs, for the hydrogen in body becomes hydrogen source material
Material, gas-liquid mixture flow up under the impetus of gas；Wherein, hydrogenation reaction is exothermic reaction, and heating jacket is to add
Hydrogen reaction heat preservation, gas-liquid mixture reach the gas-liquid separation region on reactor body top via rising passway, and hydrogen gas bubbles are de-
Reactor body is discharged by exhaust pipe from hydrogen source material, partially liq is under the driving force double action of gravity and hydrogen in liquid
It drops to reactor body bottom in decline passway to mix with new liquid hydrogen storage carrier, partially liq passes through the drain in pipeline
Reactor body is discharged in pipe.
It is hydrogen, liquid hydrogen storage carrier and catalysis that falling film reactor of the present invention, which has great response area, hydrogenation reaction,
Agent gas-liquid-solid phase reaction needs larger response area, compared with conventional tank reactor, reactor body inner wall and pipe
Pipeline outer wall is each coated with catalyst, is all to provide the region of hydrogenation reaction, improves reaction efficiency, the reaction time is reduced, to carry
High economy；Without equipment is moved in reactor body of the present invention, because hydrogenation reaction is reacted for volume-diminished, the higher reaction effect of pressure
Better, leakproofness has sizable guarantee, reduces sealing cost；The present invention uses heating jacket heat exchange mode, because adding hydrogen anti-
Exothermic reaction is should be, therefore the effect of heating jacket is not only to maintain the temperature of reaction system, while partial reaction can also be taken out of
The problems such as heat, catalyst carbon deposition inactivates caused by preventing system temperature runaway, hydrogen storage carrier coking.
In the present embodiment, the feeding device 40 includes inlet tube 41, and the inserting of inlet tube 41 is fixed on reactor body
The upper orifice of 10 bottoms and the underface for being located at liquid decline passway 70, inlet tube 41 is equipped with sealing cover, 41 upper side wall of inlet tube
Surrounding be uniformly provided with inlet opening 42.It is uniformly provided with inlet opening in inlet tube upper side wall, liquid can be made to be ejected into gas respectively
The bottom of liquid mixing rising passway, then be brought into gas-liquid mixed rising passway by gas, flowing is more uniformly effectively.
In the present embodiment, the inlet duct 50 includes air inlet pipe 51 and ring pipe 52, and air inlet pipe 51 is fixed on reaction
10 bottom of device ontology, ring pipe 52 is fixed on 51 inner end of air inlet pipe, and ring pipe 52 is connected with 51 inner end of air inlet pipe, ring pipe
Multiple ventholes 53 are along the circumferential direction provided on 52 roofs, the venthole 53 is located at the underface of gas-liquid mixed rising passway.
The redistribution of the gas in reactor will be entered by being provided with the ring pipe of multiple ventholes, enable gas even into in reactor,
And gas is input to by ring pipe in reactor body again from air inlet pipe, can increase the flow velocity of gas.
In the present embodiment, the heating jacket 20 is equipped with heat carrier import 21 and heating medium outlet 22, and the heat carries
Body import 21 is located at the top of heating jacket 20, and the heating medium outlet 22 is located at the lower part of heating jacket 20.
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-Al2O3 coatings, 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.
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 (4)
1. a kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier, including reactor body, reaction
The heating jacket of device ontology peripheral hardware promising hydrogenation reaction heat preservation is equipped with exhaust pipe at the top of reactor body, it is characterised in that：Institute
The pipeline for being equipped with and being located at immediately below exhaust pipe in reactor body is stated, the pipeline is suspended vacantly in reactor body, described
Liquid decline passway is formed in pipeline, it is logical that the gap between the pipeline and reactor body inner wall forms gas-liquid mixed rising
The side wall in road, the pipeline is equipped with deflector hole, is connected with diversion pipe at deflector hole, the free end of diversion pipe extend out to reactor
This is external, and catalyst coat is each coated on the reactor body inner wall and pipeline outer wall；The reactor body bottom is set
There is feeding device, the reactor body bottom is in the inlet duct that is arranged right below of gas-liquid mixed rising passway, the liquid
Hydrogen storage carrier is entered to from feeding device in reactor body, and hydrogen is injected into reactor body from inlet duct and by liquid
Hydrogen storage carrier is brought into gas-liquid mixed rising passway.
2. the Airlift circulating reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, including
Reactor body, it is characterised in that：The feeding device includes inlet tube, inlet tube inserting be fixed on reactor body bottom and
Positioned at the underface of liquid decline passway, the upper orifice of inlet tube is equipped with sealing cover, and the surrounding of inlet tube upper side wall is uniformly provided with
Inlet opening.
3. the Airlift circulating reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, including
Reactor body, it is characterised in that：The inlet duct includes air inlet pipe and ring pipe, and air inlet pipe is fixed on reactor body bottom
Portion, ring pipe is fixed on air inlet pipe inner end, and ring pipe is connected with air inlet pipe inner end, is along the circumferential direction opened on ring pipe roof
There are multiple ventholes, the venthole to be located at the underface of gas-liquid mixed rising passway.
4. the Airlift circulating reactor of the hydrogenation reaction according to claim 1 suitable for liquid hydrogen storage carrier, including
Reactor body, it is characterised in that：The heating jacket is equipped with heat carrier import and heating medium outlet, the heat carrier import
Positioned at the top of heating jacket, the heating medium outlet is located at the lower part of heating jacket.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810827366.4A CN108704600A (en) | 2018-07-25 | 2018-07-25 | A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810827366.4A CN108704600A (en) | 2018-07-25 | 2018-07-25 | A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108704600A true CN108704600A (en) | 2018-10-26 |
Family
ID=63875214
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810827366.4A Pending CN108704600A (en) | 2018-07-25 | 2018-07-25 | A kind of Airlift circulating reactor of hydrogenation reaction suitable for liquid hydrogen storage carrier |
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| Country | Link |
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| CN (1) | CN108704600A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109701459A (en) * | 2019-01-18 | 2019-05-03 | 淮阴工学院 | A kind of uniform inlet duct of fluidized-bed reactor |
| CN113713730A (en) * | 2021-09-13 | 2021-11-30 | 山东高密高源化工有限公司 | Be used for high-purity sodium chlorite to prepare blending device |
| WO2024096698A1 (en) * | 2022-11-03 | 2024-05-10 | 동국대학교 산학협력단 | Hydrogenation reaction system using liquid organic hydrogen carrier |
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| CN109701459A (en) * | 2019-01-18 | 2019-05-03 | 淮阴工学院 | A kind of uniform inlet duct of fluidized-bed reactor |
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Application publication date: 20181026 |