CN106701174B - liquid phase hydrogenation device and method - Google Patents
liquid phase hydrogenation device and method Download PDFInfo
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- CN106701174B CN106701174B CN201510799190.2A CN201510799190A CN106701174B CN 106701174 B CN106701174 B CN 106701174B CN 201510799190 A CN201510799190 A CN 201510799190A CN 106701174 B CN106701174 B CN 106701174B
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- 239000007791 liquid phase Substances 0.000 title claims abstract description 81
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 102
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 102
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000003054 catalyst Substances 0.000 claims abstract description 44
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 239000000203 mixture Substances 0.000 claims description 40
- 239000000446 fuel Substances 0.000 claims description 36
- 239000011229 interlayer Substances 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 6
- 239000002283 diesel fuel Substances 0.000 claims description 5
- 238000006477 desulfuration reaction Methods 0.000 claims description 4
- 230000023556 desulfurization Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 2
- 239000012071 phase Substances 0.000 claims 1
- 230000001965 increasing effect Effects 0.000 abstract description 5
- 239000013589 supplement Substances 0.000 abstract description 2
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000010410 layer Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- -1 application Chemical compound 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a liquid phase hydrogenation device and a method, wherein an upstroke reactor and a downstroke reactor are connected in series, and n catalyst bed layers and 2n-2 hydrogen supplementing points are respectively arranged in the upstroke reactor and the downstroke reactor, so that the device can be used for the reaction of raw oil with higher hydrogen consumption; at least one micropore hydrogen dissolving distributor which disperses hydrogen into microbubbles is arranged between every catalyst bed layer to carry out multipoint quantitative hydrogen supplement, so that the gas-liquid contact surface can be uniformly and effectively increased, the reaction is promoted, and the hydrogenation efficiency is improved. Meanwhile, the space between catalyst bed layers is reduced by more than 50 percent, thereby achieving the purpose of increasing the utilization efficiency of the reactor.
Description
Technical field
The present invention relates to liquid-phase hydrogenatin device and methods, belong to the device and method in hydrocarbon oil refining field in the presence of hydrogen.
Background technology
With the sustainable development of world economy and the continuous enhancing of people's environmental consciousness, fuel for cleaning vehicle is produced and used
Increasingly become a kind of development trend.China is in five standard of motor petrol state of newest publication on December 18 in 2013, by sulphur
Content is reduced to no more than 50 μ g/g no more than 10 μ g/g from state four standard.Studying gasoline, diesel deep hydrodesulfurizationof technology is
The key of fuels cleaning.
Current whole world oil refining industry is faced with crude quality and becomes poor, difficulty of processing and the increasingly increased challenge of cost.Simultaneously
Environmental protection pressure becomes to increasing, and the requirement of product quality is increasingly strict.Severe situation in face of refining oil the epoch from now on is developed more efficient anti-
It is to push the driving source of hydrogen addition technology progress to answer engineering.Hydrogenation technique is greatly developed, it is reply that efficiency, which is continuously improved, reduces energy consumption
The optimal selection of new situations.In traditional fixed bed processing technology, bulk gas is full of in reaction unit, liquid sprays downwards
Onto catalyst bed.Meanwhile being to increase mass transfer dynamics, generally use is much larger than the hydrogen-oil ratio needed for reaction, and the low stream of liquid
The consequence that speed can cause catalyst irrigation inadequate.And in liquid phase fills bed process.The hydrogen used in reaction dissolves in a liquid,
It is recycled not as gas.Therefore, the catalyst in liquid-phase hydrogenatin reaction unit is complete wet.In the catalyst and
There are liquid (catalyst with good degree of wetting) can reduce reduction catalyst active sites as far as possible around catalyst
Hot spot.Increase thermal mass and realizes that deactivation of catalyst caused by coking can be down to by these factors of complete moistened surface
Minimum level.
Chinese patent CN1488712A, CN1566281A, CN93101935.4 etc. disclose a kind of fraction oil hydrogenation refining
Method has largely hydrogen needs more than needed after the completion of hydrogenation reaction and passes through compression wherein all referring to higher hydrogen-oil ratio
Cycle plus hydrogen are carried out after machine pressurization, therefore causes the consequence of high energy consumption.
United States Patent (USP) US6428686, US6213835 etc. discloses a kind of hydrogenation technique being pre-dissolved hydrogen before reaction unit,
By mixed solvent/diluent in feedstock oil, and reach the hydrogen dissolved with high concentration, but fails to solve to remove to generate in the reaction
Hydrogen sulfide the problem of, therefore, be easy to cause reaction efficiency reduce the problem of.
Invention content
For the deficiency of existing hydrofining reaction technique, a kind of liquid-phase hydrogenatin reaction unit and method, the reaction are provided
Process can carry out the inside and outside multiple spot of reactor and quantitatively mend hydrogen, effectively increase oil gas contact, hydrogen is allow preferably to dissolve
In miscella, to improve hydrogenation reaction rate.
Meanwhile making respectively to urge instead of distribution plate and cold hydrogen line by the way that the molten hydrogen disperser of micropore is added in catalyst bed interlayer
Clearance space between agent bed reduces 50% or more, achievees the purpose that increase reactor utilization ratio.
The present invention provides a kind of liquid-phase hydrogenatin device, including heating furnace, air-fuel mixture equipment, liquid phase hydrogenation reactor, hydrogen
Air compressor, high pressure knockout drum, desulphurization plant, wherein
The air-fuel mixture equipment includes the first air-fuel mixture equipment, the second air-fuel mixture equipment；
The liquid phase hydrogenation reactor is divided into uplink liquid phase hydrogenation reactor and descending liquid phase hydrogenation reactor, and it is described on
It is connected by the second air-fuel mixture equipment between row liquid phase hydrogenation reactor and the descending liquid phase hydrogenation reactor；
The outlet line of the heating furnace is connected with the first air-fuel mixture equipment, the first air-fuel mixture equipment
Outlet is connected with the entrance of the uplink liquid phase hydrogenation reactor, outlet and the high pressure of the descending liquid phase hydrogenation reactor
Knockout drum is connected；
It is respectively provided with n catalyst bed in the uplink liquid phase hydrogenation reactor and the descending liquid phase hydrogenation reactor
Each the molten hydrogen disperser of at least one micropore that hydrogen is dispersed into microvesicle is arranged between the catalyst bed in layer；
The hydrogen gas compressor has the roads 2n hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads and the air-fuel mixture
Equipment is connected, remaining roads 2n-2 hydrogen feed pipe road connects one to one with the molten hydrogen disperser of the micropore respectively, and n is integer；
The liquid-phase hydrogenatin device further includes circulating pump, for being mixed reaction effluent as recycle oil and feedstock oil
It closes.
Liquid-phase hydrogenatin device of the present invention, wherein preferably, the high pressure knockout drum passes through an exhaust emission tube
Line is connected with the desulphurization plant.
Liquid-phase hydrogenatin device of the present invention, wherein the n is preferably 1~5.
Liquid-phase hydrogenatin device of the present invention, wherein the molten hydrogen disperser material of micropore be preferably ceramics, metal or
Membrane material.
Liquid-phase hydrogenatin device of the present invention, wherein the molten hydrogen disperser of micropore is preferably with horizontal or vertical direction
It is placed between the support plate of the catalyst bed interlayer.
The present invention also provides a kind of liquid phase hydrogenating method, which is above-mentioned liquid-phase hydrogenatin dress
It sets, includes the following steps：
High hydrogen consumption feedstock oil by heating furnace is mixed to form with hydrogen through the first air-fuel mixture equipment and mixes original
Material；
Mixed raw material is successively generated with the catalyst bed haptoreaction of the uplink liquid phase hydrogenation reactor from the bottom up
First molten hydrogen mixture, while each catalyst bed interlayer into the uplink liquid phase hydrogenation reactor injects fresh hydrogen, leads to
Cross the micropore molten hydrogen disperser fresh hydrogen is evenly dispersed at bubble；
The first molten hydrogen mixture is after the second air-fuel mixture equipment is mixed with fresh hydrogen, from top to bottom
With each catalyst bed haptoreaction reaction of formation effluent of descending liquid phase hydrogenation reactor, while adding to the descending liquid phase
Each catalyst bed interlayer of hydrogen reactor injects fresh hydrogen, by the micropore molten hydrogen disperser that fresh hydrogen is evenly dispersed
At bubble；
The reaction effluent is mixed as recycle oil with feedstock oil through high pressure knockout drum separation rear portion, another
Partial reaction effluent carries out isolated product oil.
Liquid phase hydrogenating method of the present invention, wherein the high hydrogen consumption feedstock oil is preferably straight-run diesel oil or catalysis bavin
Oil.
Liquid phase hydrogenating method of the present invention, wherein preferably, the reaction effluent is detached by the high pressure
The tail gas obtained after tank carries out desulfurization process also into desulphurization plant.
The beneficial effects of the present invention are：Liquid-phase hydrogenatin reaction response device is by being connected in series with, in entire reaction unit altogether
There are 2n layers of catalyst bed and 2n benefit hydrogen point, while also being provided with air-fuel mixture equipment outside reactor, can further supplement anti-
The hydrogen that should be consumed.Therefore, it can be used for consuming the high feedstock oil reaction of hydrogen；It, can simultaneously when handling the hydrogen lower feedstock oil of consumption
To cancel product circulation pump, further achieve the purpose that reduce investment and energy consumption；It is carried out simultaneously using the molten hydrogen disperser of micropore more
Point quantitatively mends the mode of hydrogen, to reach uniform and effectively increase gas-liquid contact face, promotes reaction, improves the mesh of hydrogenation efficiency
's.And it is equipped with support plate of the molten hydrogen disperser of micropore instead of traditional reaction unit catalyst bed interlayer in catalyst bed interlayer
Distribution plate and benefit hydrogen holes, therefore the clearance space of catalyst bed interlayer is reduced up to 50% or more, is reached and is increased reactor utilization
The purpose of efficiency；Meanwhile reaction unit of the present invention is small, wall thickness is thin, tonnage is small, has and reduces energy consumption and reduce cost
Effect.
The present invention has the following advantages：
(1) technical aspect：It can be used for diesel modifying and mitigate to deteriorate the consumption higher feedstock oil of hydrogen such as application, liquid yield
It improves, can accomplish high desulfurization rate.
(2) investing：10%-50% is saved compared to traditional hydrogen addition technology；Make instead by using the molten hydrogen distributor of micropore
It answers device volume to reduce and there is flexible draw ratio；Less floor space and steel structure platform.
(3) in terms of operating cost：25%+ is saved compared to traditional hydrogen addition technology；Heating furnace load substantially reduces；Hydrogen loss vector
Less；Device maintenance cost is lower；Catalyst amount is lower, and the practical operation service life extends.
Description of the drawings
Fig. 1 is that the upstriker reactor of the present invention connect with down-flow reactor and handles the Continuous Liquid Phase of high hydrogen consumption raw material and add
The flow chart of hydrogen process,
Wherein, reference numeral
1 entrance
2 heating furnaces
3 first air-fuel mixture equipment
4 hydrogen gas compressors
5 recycle oil pipelines
6 hydrogen make-ups are passed through the molten hydrogen disperser of micropore
7 molten hydrogen products are passed through high pressure knockout drum
8 high pressure knockout drums
9 high pressure separation products are passed through desulphurization plant
10 desulphurization plants
11 product oil pipelines
12 circulating pumps
13 uplink liquid phase hydrogenation reactors
14 descending liquid phase hydrogenation reactors
15 second air-fuel mixture equipment；
Fig. 2 is structural schematic diagram of the liquid-phase hydrogenatin reaction unit of the present invention when micropore dispersion device is vertically arranged.
Specific implementation mode
Technical solution of the present invention is described in detail in the following with reference to the drawings and specific embodiments, to be further understood that
The purpose of the present invention, scheme and effect, but it is not intended as the limitation of scope of the appended claims of the present invention.
Refering to fig. 1, liquid-phase hydrogenatin device provided in this embodiment, including heating furnace 2, air-fuel mixture equipment, liquid-phase hydrogenatin
Reactor, hydrogen gas compressor 4, high pressure knockout drum 8, desulphurization plant 10, wherein
The air-fuel mixture equipment includes the first air-fuel mixture equipment 3, the second air-fuel mixture equipment 15；
The liquid phase hydrogenation reactor is divided into uplink liquid phase hydrogenation reactor 13 and descending liquid phase hydrogenation reactor 14, and institute
It states between uplink liquid phase hydrogenation reactor 13 and the descending liquid phase hydrogenation reactor 14 through the second air-fuel mixture equipment
15 series connection；
The outlet line of the heating furnace 2 is connected with the first air-fuel mixture equipment 3, the first air-fuel mixture equipment
3 outlet is connected with the entrance of the uplink liquid phase hydrogenation reactor 13, the outlet of the descending liquid phase hydrogenation reactor 14 with
The high pressure knockout drum 8 is connected；
It is respectively provided with n catalyst in the uplink liquid phase hydrogenation reactor 13 and the descending liquid phase hydrogenation reactor 14
Each the molten hydrogen disperser of at least one micropore that hydrogen is dispersed into microvesicle is arranged between the catalyst bed in bed；
The hydrogen gas compressor 4 has the roads 2n hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads and the air-fuel mixture
Equipment is connected, remaining roads 2n-2 hydrogen feed pipe road connects one to one with the molten hydrogen disperser of the micropore respectively, and n is integer,
In the present embodiment, 2 n；Certainly, n may be 3 either 4 or 5 in other embodiments；
The liquid-phase hydrogenatin device further includes circulating pump 12, for being mixed reaction effluent as recycle oil and feedstock oil
It closes, because the raw material of processing is that high hydrogen consumes raw material, therefore the liquid-phase hydrogenatin reaction system further includes having to connect with raw material oil-in 1
Recycle oil pipeline 5, high pressure knockout drum 8 are connect by circulating pump 12 with recycle oil pipeline.
The high pressure knockout drum 8 is connected by an exhaust emission tube line with the desulphurization plant 10.
The molten hydrogen disperser material of micropore is ceramics, and the molten hydrogen disperser material of micropore can be in other embodiments certainly
It is metal or membrane material, the molten hydrogen disperser of micropore is placed in horizontal direction between the support plate of the catalyst bed interlayer；Certainly exist
The molten hydrogen disperser of micropore can be placed in vertical direction between the support plate of the catalyst bed interlayer in other embodiment.
It should be noted that, although the catalyst bed in liquid phase hydrogenation reactor shown in Fig. 1 is two, but in reality
It is not limited thereto in the application of border, the number n of the catalyst bed in every section can be 1~5.
Referring to Fig.2, the molten hydrogen disperser of micropore that the liquid-phase hydrogenatin reaction unit of the present invention is built in catalyst bed interlayer is perpendicular
Disposed upright eliminates distribution plate and cold hydrogen tube between the support plate and lower catalyst agent top spacer of overlying catalyst.
The liquid phase hydrogenating method that the present embodiment also provides, the liquid phase hydrogenating method are to utilize above-mentioned liquid-phase hydrogenatin device, packet
Include following steps：
It will be mixed to form mixed raw material through the first air-fuel mixture equipment with hydrogen by the straight-run diesel oil of heating furnace, when
So in other embodiments, it can be catalytic diesel oil is mixed to form mixed raw material with hydrogen through the first air-fuel mixture equipment；
Mixed raw material is successively generated with the catalyst bed haptoreaction of the uplink liquid phase hydrogenation reactor from the bottom up
First molten hydrogen mixture, while each catalyst bed interlayer into the uplink liquid phase hydrogenation reactor injects fresh hydrogen, leads to
Cross the micropore molten hydrogen disperser fresh hydrogen is evenly dispersed at bubble；
The first molten hydrogen mixture is after the second air-fuel mixture equipment is mixed with fresh hydrogen, from top to bottom
With each catalyst bed haptoreaction reaction of formation effluent of descending liquid phase hydrogenation reactor, while adding to the descending liquid phase
Each catalyst bed interlayer of hydrogen reactor injects fresh hydrogen, by the micropore molten hydrogen disperser that fresh hydrogen is evenly dispersed
At bubble；
The reaction effluent is mixed as recycle oil with feedstock oil through high pressure knockout drum separation rear portion, another
Partial reaction effluent carries out isolated product oil, and obtained tail gas carries out desulfurization process also into desulphurization plant.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
It knows those skilled in the art and makes various corresponding change and deformations, but these corresponding changes and change in accordance with the present invention
Shape should all belong to the protection domain of appended claims of the invention.
Claims (8)
1. a kind of liquid-phase hydrogenatin device, including heating furnace, air-fuel mixture equipment, liquid phase hydrogenation reactor, hydrogen gas compressor, high pressure
Knockout drum, desulphurization plant, which is characterized in that
The air-fuel mixture equipment includes the first air-fuel mixture equipment, the second air-fuel mixture equipment；
The liquid phase hydrogenation reactor is divided into uplink liquid phase hydrogenation reactor and descending liquid phase hydrogenation reactor, and the uplink liquid
It is connected by the second air-fuel mixture equipment between phase hydrogenation reactor and the descending liquid phase hydrogenation reactor；
The outlet line of the heating furnace is connected with the first air-fuel mixture equipment, the outlet of the first air-fuel mixture equipment
It is connected with the entrance of the uplink liquid phase hydrogenation reactor, the outlet of the descending liquid phase hydrogenation reactor is detached with the high pressure
Tank is connected；
It is respectively provided with n catalyst bed in the uplink liquid phase hydrogenation reactor and the descending liquid phase hydrogenation reactor, often
The molten hydrogen disperser of at least one micropore that hydrogen is dispersed into microvesicle is set between a catalyst bed；
The hydrogen gas compressor has the roads 2n hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads and the air-fuel mixture equipment
It is connected, remaining roads 2n-2 hydrogen feed pipe road connects one to one with the molten hydrogen disperser of the micropore respectively, and n is integer；
The liquid-phase hydrogenatin device further includes circulating pump, for mixing reaction effluent as recycle oil with feedstock oil.
2. liquid-phase hydrogenatin device according to claim 1, which is characterized in that the high pressure knockout drum is discharged by a tail gas
Pipeline is connected with the desulphurization plant.
3. liquid-phase hydrogenatin device according to claim 1 or 2, which is characterized in that the n is 1~5.
4. liquid-phase hydrogenatin device according to claim 1 or 2, which is characterized in that the molten hydrogen disperser material of micropore is
Ceramics, metal or membrane material.
5. liquid-phase hydrogenatin device according to claim 1 or 2, which is characterized in that the molten hydrogen disperser of micropore is with level
Or vertical direction is placed between the support plate of the catalyst bed interlayer.
6. a kind of liquid phase hydrogenating method, which is the liquid-phase hydrogenatin of any one of Claims 1 to 5
Device includes the following steps：
High hydrogen consumption feedstock oil by heating furnace is mixed to form mixed raw material with hydrogen through the first air-fuel mixture equipment；
Mixed raw material successively generates first with the catalyst bed haptoreaction of the uplink liquid phase hydrogenation reactor from the bottom up
Molten hydrogen mixture, while each catalyst bed interlayer into the uplink liquid phase hydrogenation reactor injects fresh hydrogen, passes through institute
State micropore molten hydrogen disperser fresh hydrogen is evenly dispersed at bubble；
The first molten hydrogen mixture is after the second air-fuel mixture equipment is mixed with fresh hydrogen, from top to bottom under
Each catalyst bed haptoreaction reaction of formation effluent of row liquid phase hydrogenation reactor, while adding hydrogen anti-to the descending liquid phase
Each catalyst bed interlayer of device is answered to inject fresh hydrogen, it is by the micropore molten hydrogen disperser that fresh hydrogen is evenly dispersed at gas
Bubble；
The reaction effluent is mixed as recycle oil with feedstock oil through high pressure knockout drum separation rear portion, another part
Reaction effluent carries out isolated product oil.
7. liquid phase hydrogenating method according to claim 6, which is characterized in that the high hydrogen consumption feedstock oil be straight-run diesel oil or
Catalytic diesel oil.
8. the liquid phase hydrogenating method described according to claim 6 or 7, which is characterized in that the reaction effluent passes through the height
The tail gas obtained after pressure knockout drum carries out desulfurization process also into desulphurization plant.
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|---|---|---|---|
| CN201510799190.2A CN106701174B (en) | 2015-11-18 | 2015-11-18 | liquid phase hydrogenation device and method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510799190.2A CN106701174B (en) | 2015-11-18 | 2015-11-18 | liquid phase hydrogenation device and method |
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| CN106701174A CN106701174A (en) | 2017-05-24 |
| CN106701174B true CN106701174B (en) | 2018-08-14 |
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| CN112705122B (en) * | 2019-10-25 | 2022-07-08 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reactor and hydrogenation method |
| CN111871337A (en) * | 2020-07-16 | 2020-11-03 | 南京延长反应技术研究院有限公司 | Micro-interface reaction system and method for diesel hydrogenation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102002395A (en) * | 2010-12-08 | 2011-04-06 | 华东理工大学 | Method and device for dissolving gas in liquid-phase circulating hydrodesulfurization system |
| CN203238222U (en) * | 2013-04-03 | 2013-10-16 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system |
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
-
2015
- 2015-11-18 CN CN201510799190.2A patent/CN106701174B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102002395A (en) * | 2010-12-08 | 2011-04-06 | 华东理工大学 | Method and device for dissolving gas in liquid-phase circulating hydrodesulfurization system |
| CN203238222U (en) * | 2013-04-03 | 2013-10-16 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reaction device with multistage hydrogen dissolving system |
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
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