CN106701180A - Liquid phase hydrogenation device and method - Google Patents
Liquid phase hydrogenation device and method Download PDFInfo
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- CN106701180A CN106701180A CN201510794986.9A CN201510794986A CN106701180A CN 106701180 A CN106701180 A CN 106701180A CN 201510794986 A CN201510794986 A CN 201510794986A CN 106701180 A CN106701180 A CN 106701180A
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- Prior art keywords
- hydrogen
- liquid phase
- hydrogenation reactor
- phase hydrogenation
- fuel mixture
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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 59
- 238000000034 method Methods 0.000 title claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 99
- 239000001257 hydrogen Substances 0.000 claims abstract description 99
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 238000006243 chemical reaction Methods 0.000 claims abstract description 35
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 33
- 239000003054 catalyst Substances 0.000 claims abstract description 27
- 239000000203 mixture Substances 0.000 claims description 39
- 239000000446 fuel Substances 0.000 claims description 35
- 239000003921 oil Substances 0.000 claims description 24
- 239000011229 interlayer Substances 0.000 claims description 14
- 239000000463 material Substances 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 5
- 239000010687 lubricating oil Substances 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 239000003350 kerosene Substances 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 15
- 230000001965 increasing effect Effects 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 6
- 239000013589 supplement Substances 0.000 abstract description 2
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 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
- 239000003502 gasoline 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
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007812 deficiency Effects 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
- 239000010410 layer Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur 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
- 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
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, in particular to a continuous liquid phase hydrogenation process method without product circulation by connecting a downlink reactor and an uplink reactor in series, wherein the downlink reactor and the uplink reactor are respectively provided with n catalyst bed layers and 2n-2 hydrogen supplementing points, and 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 hydrocarbon oil refining field in the presence of hydrogen, more particularly to a kind of Continuous Liquid Phase hydrogenation technique side
Method.
Background technology
With the sustainable development and the continuous enhancing of people's environmental consciousness of World Economics, cleaning car is produced and used
A kind of development trend is increasingly becomed with fuel.China is automobile-used the newest issue of December 18 in 2013
In the standard of gasoline state five, sulfur content is not more than 50 μ g/g from state four standard and is reduced to no more than 10 μ
g/g.Research gasoline, diesel deep hydrodesulfurizationof technology is the key of fuels cleaning.
Whole world oil refining industry is faced with crude quality and becomes poor at present, difficulty of processing and cost is increasingly increased chooses
War.Environmental protection pressure becomes to increasing simultaneously, and the requirement of product quality is increasingly strict.Sternness in face of refining oil the epoch from now on
Situation, it is the driving source for promoting hydrogen addition technology progress to develop more efficient reaction engineering.Greatly develop hydrogenation work
Skill, it is to tackle the optimal selection of new situations to improve constantly efficiency, reducing energy consumption.Processed in traditional fixed bed
In technique, a large amount of gases are full of in reaction unit, liquid is sprayed onto beds downwards.Meanwhile, it is
Mass transfer dynamics is increased, generally using the hydrogen-oil ratio needed for being much larger than reaction, and liquid low flow velocity can cause catalysis
Agent soaks inadequate consequence.And in liquid phase filling bed process.The hydrogen used in reaction dissolves in a liquid,
It is circulated not as gas.Therefore, the catalyst in liquid-phase hydrogenatin reaction unit is complete wet.
There is liquid (having the catalyst of good degree of wetting) in catalyst and around catalyst can be as far as possible
Reduce the focus for reducing catalyst active sites.Increase thermal mass simultaneously realizes that complete moistened surface these factors can
Degree is minimized with the deactivation of catalyst for causing coking.
Chinese patent CN1488712A, CN1566281A, CN93101935.4 etc. disclose a kind of cut
Oily hydrofinishing process, wherein all refer to hydrogen-oil ratio higher, has substantial amounts of after the completion of hydrogenation reaction
Hydrogen more than needed needs to be circulated hydrogenation after compressor pressurizes, and has thus resulted in the consequence of high energy consumption.
United States Patent (USP) US6428686, US6213835 etc. disclose it is a kind of be pre-dissolved before reaction unit hydrogen plus
Hydrogen technique, by mixed solvent/diluent in feedstock oil, and reaches the hydrogen dissolved with high concentration, but fail
The hydrogen sulfide that removing is generated in the reaction is solved the problems, such as, therefore, easily cause the problem of reaction efficiency reduction.
The content of the invention
For the deficiency of existing hydrofining reaction technique, there is provided a kind of liquid-phase hydrogenatin course of reaction, the reaction
Process can carry out the inside and outside multiple spot of reactor and quantitatively mend hydrogen, effectively increase oil gas contact, make the hydrogen can
To be preferably dissolved in miscella, so as to improve hydrogenation reaction speed.
Meanwhile, the molten hydrogen disperser of micropore is added by catalyst bed interlayer, distribution plate and cold hydrogen line are instead of,
The clearance space of each catalyst bed interlayer is reduced more than 50%, reach the mesh for increasing reactor utilization ratio
's.
The present invention provides a kind of liquid-phase hydrogenatin device, including heating furnace, air-fuel mixture equipment, liquid-phase hydrogenatin are anti-
Device, hydrogen gas compressor, high pressure knockout drum, desulphurization plant are answered, 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 up liquid phase hydrogenation reactor, institute
Descending liquid phase hydrogenation reactor is stated to be set by second air-fuel mixture with the up liquid phase hydrogenation reactor
Standby series connection；
The outlet line of the heating furnace is connected with the first air-fuel mixture equipment, first air-fuel mixture
The outlet of equipment is connected with the entrance of the descending liquid phase hydrogenation reactor, the up liquid phase hydrogenation reactor
Outlet be connected with the high pressure knockout drum；
There is n respectively in the descending liquid phase hydrogenation reactor and the up liquid phase hydrogenation reactor to urge
Agent bed, sets at least one micropore that hydrogen is dispersed into microvesicle molten between each described beds
Hydrogen disperser；
The hydrogen gas compressor has 2n roads hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads with it is described
Air-fuel mixture equipment be connected, remaining 2n-2 roads hydrogen feed pipe road respectively with the molten hydrogen disperser one of the micropore
One correspondence connection, n is integer.
Liquid-phase hydrogenatin device of the present invention, these, it is preferred to, the high pressure knockout drum passes through a tail
Gas discharge pipe 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 preferably with level or hangs down
Nogata is between the support plate for being placed in the catalyst bed interlayer.
The present invention also provides a kind of liquid phase hydrogenating method, and the liquid phase hydrogenating method equipment therefor is that above-mentioned liquid phase adds
Hydrogen production device, comprises the following steps：
To be mixed to form through the first air-fuel mixture equipment with hydrogen by the low hydrogen of heating furnace consumption feedstock oil
Mixed material；
Mixed material is successively contacted instead with the beds of the descending liquid phase hydrogenation reactor from top to bottom
The first molten hydrogen mixture should be generated, while to each catalyst bed interlayer in the descending liquid phase hydrogenation reactor
Injection fresh hydrogen, it is by the micropore molten hydrogen disperser that fresh hydrogen is dispersed into bubble；
The first molten hydrogen mixture after the second air-fuel mixture equipment mixes with fresh hydrogen, from
Under up with each beds haptoreaction reaction of formation effluent of up liquid phase hydrogenation reactor, while
Fresh hydrogen is injected to each catalyst bed interlayer of the up liquid phase hydrogenation reactor, it is molten by the micropore
Hydrogen disperser is dispersed into bubble by fresh hydrogen；
The reaction effluent obtains product oil after being separated through the high pressure knockout drum.
Liquid phase hydrogenating method of the present invention, wherein, the low hydrogen consumption feedstock oil is preferably straight run boat kerosene
Product, reformed pre-hydrogenated oil product, lube oil hydrogenation isomery oil product, because the raw material for processing is for low hydrogen consumes raw material, instead
Effluent is answered not to be circulated.
Liquid phase hydrogenating method of the present invention, these, it is preferred to, the reaction effluent is by described
The tail gas obtained after high pressure knockout drum carries out desulfurization process also into desulphurization plant.
The beneficial effects of the present invention are：By being connected in series, whole reaction is filled liquid-phase hydrogenatin reaction response device
Interior total 2n layers of beds and 2n benefit hydrogen point are put, while air-fuel mixture also is provided with outside reactor setting
It is standby, can further supplement the hydrogen of reaction consumption.Therefore, it can the feedstock oil reaction high for consuming hydrogen；Together
When processing hydrogen and consuming relatively low feedstock oil, product circulation pump can be cancelled, further up to reduce investment and
The purpose of energy consumption；Carried out by the way of multiple spot quantitatively mends hydrogen using the molten hydrogen disperser of micropore simultaneously, so as to reach
Even and effectively increase gas-liquid contact face, promotion reaction, improves the purpose of hydrogenation efficiency.And, in catalyst
The support plate distribution that the molten hydrogen disperser of micropore instead of traditional reaction unit catalyst bed interlayer is provided between bed
Disk and mend hydrogen holes, therefore catalyst bed interlayer clearance space reduce up to more than 50%, reach increase reaction
The purpose of device utilization ratio；Meanwhile, reaction unit small volume of the present invention, wall thickness are thin, tonnage is small,
With the effect for reducing energy consumption reduces cost.
The present invention has advantages below：
(1) technical elements：Can be used for straight run boat coal, reformed pre-hydrogenated and lube oil hydrogenation isomery etc. low
The reaction of hydrogen consumption, while cancelling product circulation, reaction process is greatly simplified.
(2) investing：10%-50% is saved compared to traditional hydrogen addition technology；Distributed by using the molten hydrogen of micropore
The reaction unit volume that device makes is reduced and with flexible draw ratio；Less floor space and steel construction are flat
Platform.
(3) operating cost aspect：25%+ is saved compared to traditional hydrogen addition technology；Heating furnace load is substantially reduced；
Hydrogen loss vector is less；Device maintenance cost is lower；Catalyst amount is lower, practical operation life.
Brief description of the drawings
Fig. 1 be down-flow reactor of the invention connected with upstriker reactor treatment low hydrogen consume raw material company
The flow chart of continuous liquid-phase hydrogenation processing method,
Wherein, reference
1 entrance
2 heating furnaces
3 first air-fuel mixture equipment
4 hydrogen gas compressors
5 product 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 descending liquid phase hydrogenation reactors
12 up liquid phase hydrogenation reactors
13 second air-fuel mixture equipment；
Fig. 2 is structural representation of the liquid-phase hydrogenatin reaction unit of the invention when micropore dispersion device is vertically arranged.
Specific embodiment
Technical solution of the present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings, more to enter one
Step understands the purpose of the present invention, scheme and effect, but is not intended as scope of the appended claims of the present invention
Limitation.
Refering to Fig. 1, the liquid-phase hydrogenatin device in the present embodiment, including heating furnace 2, air-fuel mixture equipment,
Liquid phase hydrogenation 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 13；
The liquid phase hydrogenation reactor is divided into descending liquid phase hydrogenation reactor 11 with up liquid phase hydrogenation reactor
12, the descending liquid phase hydrogenation reactor 11 passes through described second with the up liquid phase hydrogenation reactor 12
Air-fuel mixture equipment 13 is connected；
The outlet line of the heating furnace 2 is connected with the first air-fuel mixture equipment 3, first oil gas
The outlet of mixing apparatus 3 is connected with the entrance of the descending liquid phase hydrogenation reactor 11, the up liquid phase
The outlet of hydrogenation reactor 12 is connected with the high pressure knockout drum 8；
There is n respectively in the descending liquid phase hydrogenation reactor 11 and the up liquid phase hydrogenation reactor 12
Individual beds, set at least one and hydrogen are dispersed into the micro- of microvesicle between each described beds
The molten hydrogen disperser in hole；
The hydrogen gas compressor has 2n roads hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads with it is described
Air-fuel mixture equipment be connected, remaining 2n-2 roads hydrogen feed pipe road respectively with the molten hydrogen disperser one of the micropore
One correspondence connection, n is integer, and in the present embodiment, n is 2；Certainly, n in other embodiments
Can be 3 or 4 or 5；
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 of micropore disperses equipment in other embodiments certainly
Material can be metal or membrane material, and the molten hydrogen disperser of micropore is placed in the catalyst bed interlayer with horizontal direction
Between support plate；Certainly the molten hydrogen disperser of micropore can be placed in the catalysis with vertical direction in other embodiments
Between the support plate between agent bed.
It should be noted that, although the beds in the liquid phase hydrogenation reactor shown in Fig. 1 are two
It is individual, but be not limited thereto in actual applications, the number n of the beds in every section can be 1~5.
Refering to Fig. 2, the molten hydrogen of micropore that liquid-phase hydrogenatin reaction unit of the invention is built in catalyst bed interlayer point
Scattered device is vertically placed between the support plate of overlying catalyst and lower catalyst agent top spacer, eliminates distribution
Disk and cold hydrogen tube.
Liquid phase hydrogenating method in the present embodiment, the liquid phase hydrogenating method is to utilize above-mentioned liquid-phase hydrogenatin device,
Comprise the following steps：
To be mixed to form through the first air-fuel mixture equipment with hydrogen by the straight run of heating furnace boat kerosene product
Mixed material；Certainly, can also be in other embodiments that reformed pre-hydrogenated oil product or lube oil hydrogenation are different
Structure oil product is mixed to form mixed material with hydrogen through the first air-fuel mixture equipment；Because the raw material for processing is low
Hydrogen consumes raw material, and reaction effluent is not circulated；
Mixed material is successively contacted instead with the beds of the descending liquid phase hydrogenation reactor from top to bottom
The first molten hydrogen mixture should be generated, while to each catalyst bed interlayer in the descending liquid phase hydrogenation reactor
Injection fresh hydrogen, it is by the micropore molten hydrogen disperser that fresh hydrogen is dispersed into bubble；
The first molten hydrogen mixture after the second air-fuel mixture equipment mixes with fresh hydrogen, from
Under up with each beds haptoreaction reaction of formation effluent of up liquid phase hydrogenation reactor, while
Fresh hydrogen is injected to each catalyst bed interlayer of the up liquid phase hydrogenation reactor, it is molten by the micropore
Hydrogen disperser is dispersed into bubble by fresh hydrogen；
The reaction effluent through the high pressure knockout drum separate after obtain product oil, the tail gas for obtaining also into
Desulphurization plant carries out desulfurization process.
Certainly, the present invention can also have other various embodiments, in the feelings without departing substantially from spirit of the invention and its essence
Under condition, those of ordinary skill in the art work as can make various corresponding changes and deformation according to the present invention, but
These corresponding changes and deformation 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, it is characterised 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 up liquid phase hydrogenation reactor, institute
Descending liquid phase hydrogenation reactor is stated to be set by second air-fuel mixture with the up liquid phase hydrogenation reactor
Standby series connection；
The outlet line of the heating furnace is connected with the first air-fuel mixture equipment, first air-fuel mixture
The outlet of equipment is connected with the entrance of the descending liquid phase hydrogenation reactor, the up liquid phase hydrogenation reactor
Outlet be connected with the high pressure knockout drum；
There is n respectively in the descending liquid phase hydrogenation reactor and the up liquid phase hydrogenation reactor to urge
Agent bed, sets at least one micropore that hydrogen is dispersed into microvesicle molten between each described beds
Hydrogen disperser；
The hydrogen gas compressor has 2n roads hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads with it is described
Air-fuel mixture equipment be connected, remaining 2n-2 roads hydrogen feed pipe road respectively with the molten hydrogen disperser one of the micropore
One correspondence connection, n is integer.
2. liquid-phase hydrogenatin device according to claim 1, it is characterised in that the high pressure knockout drum
It is connected with the desulphurization plant by an exhaust emission tube line.
3. liquid-phase hydrogenatin device according to claim 1 and 2, it is characterised in that the n is 1~5.
4. liquid-phase hydrogenatin device according to claim 1 and 2, it is characterised in that the micropore is molten
Hydrogen disperser material is ceramics, metal or membrane material.
5. liquid-phase hydrogenatin device according to claim 1 and 2, it is characterised in that the micropore is molten
Between hydrogen disperser is placed in the support plate of the catalyst bed interlayer with horizontal or vertical direction.
6. a kind of liquid phase hydrogenating method, the liquid phase hydrogenating method equipment therefor is any one of Claims 1 to 5
The liquid-phase hydrogenatin device, comprises the following steps：
To be mixed to form through the first air-fuel mixture equipment with hydrogen by the low hydrogen of heating furnace consumption feedstock oil
Mixed material；
Mixed material is successively contacted instead with the beds of the descending liquid phase hydrogenation reactor from top to bottom
The first molten hydrogen mixture should be generated, while to each catalyst bed interlayer in the descending liquid phase hydrogenation reactor
Injection fresh hydrogen, it is by the micropore molten hydrogen disperser that fresh hydrogen is dispersed into bubble；
The first molten hydrogen mixture after the second air-fuel mixture equipment mixes with fresh hydrogen, from
Under up with each beds haptoreaction reaction of formation effluent of up liquid phase hydrogenation reactor, while
Fresh hydrogen is injected to each catalyst bed interlayer of the up liquid phase hydrogenation reactor, it is molten by the micropore
Hydrogen disperser is dispersed into bubble by fresh hydrogen；
The reaction effluent obtains product oil after being separated through the high pressure knockout drum.
7. liquid phase hydrogenating method according to claim 6, it is characterised in that the low hydrogen consumes raw material
Oil is straight run boat kerosene product, reformed pre-hydrogenated oil product, lube oil hydrogenation isomery oil product.
8. the liquid phase hydrogenating method according to claim 6 or 7, it is characterised in that the reaction stream
Go out thing carries out desulfurization process by the tail gas obtained after the high pressure knockout drum also into desulphurization plant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510794986.9A CN106701180B (en) | 2015-11-18 | 2015-11-18 | liquid phase hydrogenation device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510794986.9A CN106701180B (en) | 2015-11-18 | 2015-11-18 | liquid phase hydrogenation device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106701180A true CN106701180A (en) | 2017-05-24 |
| CN106701180B CN106701180B (en) | 2018-09-04 |
Family
ID=58933497
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510794986.9A Active CN106701180B (en) | 2015-11-18 | 2015-11-18 | liquid phase hydrogenation device and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109731532A (en) * | 2019-03-07 | 2019-05-10 | 湖南中天元环境工程有限公司 | A kind of hydrocarbon oil hydrogenation reactor and method for hydrotreating hydrocarbon oil |
| CN114409502A (en) * | 2020-10-09 | 2022-04-29 | 中石化南京化工研究院有限公司 | Synthesis process for preparing 1, 10-decanediol from dimethyl sebacate through hydrogenation at low hydrogen ester ratio |
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| US20040238409A1 (en) * | 2003-05-30 | 2004-12-02 | Harjeet Virdi | Hydrogenation of middle distillate using a counter-current reactor |
| 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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2015
- 2015-11-18 CN CN201510794986.9A patent/CN106701180B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040238409A1 (en) * | 2003-05-30 | 2004-12-02 | Harjeet Virdi | Hydrogenation of middle distillate using a counter-current reactor |
| 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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109731532A (en) * | 2019-03-07 | 2019-05-10 | 湖南中天元环境工程有限公司 | A kind of hydrocarbon oil hydrogenation reactor and method for hydrotreating hydrocarbon oil |
| CN114409502A (en) * | 2020-10-09 | 2022-04-29 | 中石化南京化工研究院有限公司 | Synthesis process for preparing 1, 10-decanediol from dimethyl sebacate through hydrogenation at low hydrogen ester ratio |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106701180B (en) | 2018-09-04 |
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