CN106701179B - Liquid-phase hydrogenatin device and method - Google Patents
Liquid-phase hydrogenatin device and method Download PDFInfo
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- CN106701179B CN106701179B CN201510794632.4A CN201510794632A CN106701179B CN 106701179 B CN106701179 B CN 106701179B CN 201510794632 A CN201510794632 A CN 201510794632A CN 106701179 B CN106701179 B CN 106701179B
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
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- 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 present invention relates to a kind of liquid-phase hydrogenatin device and methods, specifically it is connected in series with using down-flow reactor and upstriker reactor, it is respectively provided with 2 benefit hydrogen points of n catalyst bed and 2n in down-flow reactor and upstriker reactor, can be used for consuming the higher feedstock oil reaction of hydrogen；Hydrogen is dispersed into the molten hydrogen distributor of micropore of microvesicle by each catalyst bed interlayer setting at least one, is carried out the mode that multiple spot quantitatively mends hydrogen, can uniformly and effectively be increased gas-liquid contact face, promote reaction, improves hydrogenation efficiency.The clearance space of each catalyst bed interlayer reduces 50% or more simultaneously, achievees the purpose that increase reactor utilization ratio.
Description
Technical field
The present invention relates to hydrocarbon oil refining field in the presence of hydrogen, more particularly to a kind of Continuous Liquid Phase hydrogenation method.
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 process is provided, which can
Hydrogen is quantitatively mended to carry out the inside and outside multiple spot of reactor, effectively increases oil gas contact, hydrogen is allow preferably to be dissolved in mixing
In oil, 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 descending liquid phase hydrogenation reactor and uplink liquid phase hydrogenation reactor, and it is described under
It is connected by the second air-fuel mixture equipment between row liquid phase hydrogenation reactor and the uplink 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 descending liquid phase hydrogenation reactor, outlet and the high pressure of the uplink liquid phase hydrogenation reactor
Knockout drum is connected；
It is respectively provided with n catalyst bed in the descending liquid phase hydrogenation reactor and the uplink 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 descending liquid phase hydrogenation reactor from top to bottom
First molten hydrogen mixture, while each catalyst bed interlayer into the descending 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 the bottom up
With each catalyst bed haptoreaction reaction of formation effluent of uplink liquid phase hydrogenation reactor, while adding to the uplink 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, because the raw material of processing is that high hydrogen consumes raw material, therefore a part of reaction effluent is mixed as recycle oil with feedstock oil, another portion
Reaction effluent is divided to carry out isolated product 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 down-flow reactor of the present invention connect with upstriker 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 descending liquid phase hydrogenation reactors
14 uplink 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.
With reference to attached drawing 1, the liquid-phase hydrogenatin device in the present 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 descending liquid phase hydrogenation reactor 13 and uplink liquid phase hydrogenation reactor 14, and institute
It states between descending liquid phase hydrogenation reactor 13 and the uplink 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 descending liquid phase hydrogenation reactor 13, the outlet of the uplink liquid phase hydrogenation reactor 14 with
The high pressure knockout drum 8 is connected；
It is respectively provided with n catalyst in the descending liquid phase hydrogenation reactor 13 and the uplink 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 descending liquid phase hydrogenation reactor from top to bottom
First molten hydrogen mixture, while each catalyst bed interlayer into the descending 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 the bottom up
With each catalyst bed haptoreaction reaction of formation effluent of uplink liquid phase hydrogenation reactor, while adding to the uplink 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 descending liquid phase hydrogenation reactor and uplink liquid phase hydrogenation reactor, and the downlink liquid
It is connected by the second air-fuel mixture equipment between phase hydrogenation reactor and the uplink 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 descending liquid phase hydrogenation reactor, the outlet of the uplink liquid phase hydrogenation reactor is detached with the high pressure
Tank is connected；
It is respectively provided with n catalyst bed in the descending liquid phase hydrogenation reactor and the uplink 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 descending liquid phase hydrogenation reactor from top to bottom
Molten hydrogen mixture, while each catalyst bed interlayer into the descending 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 after the second air-fuel mixture equipment is mixed with fresh hydrogen, from the bottom up with it is upper
Each catalyst bed haptoreaction reaction of formation effluent of row liquid phase hydrogenation reactor, at the same it is anti-to the uplink liquid-phase hydrogenatin
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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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107987011A (en) * | 2017-12-12 | 2018-05-04 | 安徽国星生物化学有限公司 | A kind of piperidines is continuously synthesizing to method |
| CN111686645A (en) * | 2019-03-15 | 2020-09-22 | 南京延长反应技术研究院有限公司 | Micro-interface reinforced wax oil hydrogenation reaction system and method |
| CN111686644A (en) * | 2019-03-15 | 2020-09-22 | 南京延长反应技术研究院有限公司 | Descending type fixed bed oil product hydrogenation micro-interface strengthening reaction system |
| CN111530380B (en) * | 2019-03-15 | 2021-02-02 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced reaction system and method for preparing ship fuel by heavy oil hydrogenation |
| CN112705119B (en) * | 2019-10-25 | 2022-06-07 | 中国石油化工股份有限公司 | Heavy oil 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 |
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| 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 multi-grade 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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| US7247235B2 (en) * | 2003-05-30 | 2007-07-24 | Abb Lummus Global Inc, | Hydrogenation of middle distillate using a counter-current reactor |
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| 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 multi-grade 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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