CN106701179A - Liquid phase hydrogenation device and method - Google Patents
Liquid phase hydrogenation device and method Download PDFInfo
- Publication number
- CN106701179A CN106701179A CN201510794632.4A CN201510794632A CN106701179A CN 106701179 A CN106701179 A CN 106701179A CN 201510794632 A CN201510794632 A CN 201510794632A CN 106701179 A CN106701179 A CN 106701179A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- liquid phase
- hydrogenation reactor
- phase hydrogenation
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- 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
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. According to the liquid phase hydrogenation device, a down flow reactor and an up flow reactor are connected in series; each of the down flow reactor and the up flow reactor comprises n catalyst beds and 2n-2 hydrogen supplying points; and the liquid phase hydrogenation device can be used for raw oil reaction high in hydrogen consumption; each catalyst bed is provided with a micropore hydrogen dissolving distributor used for dispersing hydrogen into microbubbles, multipoint quantitative hydrogen supplying is adopted, gas-liquid contact area is enlarged uniformly and effectively, reaction is promoted, hydrogenation efficiency is increased, the space between each pair of catalyst beds is reduced by more than 50%, and reactor utilization efficiency is increased.
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, and
Pass through second oil gas between the descending liquid phase hydrogenation reactor and the up liquid phase hydrogenation reactor
Mixing apparatus is connected；
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；
The liquid-phase hydrogenatin device also includes circulating pump, for using reaction effluent as recycle oil and raw material
Oil mixing.
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 hydrogen high 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 separates rear portion and is mixed as recycle oil and feedstock oil through the high pressure knockout drum
Close, another part reaction effluent carries out isolated product oil.
Liquid phase hydrogenating method of the present invention, wherein, the hydrogen high consumption feedstock oil be preferably straight-run diesel oil or
Catalytic diesel oil, because process raw material for hydrogen high consume raw material, therefore a part of reaction effluent as recycle oil with
Feedstock oil mixes, and another part reaction effluent carries out isolated product oil.
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 diesel modifying and relax the consumption hydrogen such as deterioration application feedstock oil higher,
Liquid yield is improved, and can accomplish high desulfurization rate.
(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 is that down-flow reactor of the invention treatment hydrogen high of being connected with upstriker reactor consumes the company of raw material
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 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 up liquid phase hydrogenation reactors
15 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.
Referring to the drawings 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 15；
The liquid phase hydrogenation reactor is divided into descending liquid phase hydrogenation reactor 13 with up liquid phase hydrogenation reactor
Pass through institute between 14, and the descending liquid phase hydrogenation reactor 13 and the up liquid phase hydrogenation reactor 14
The second air-fuel mixture equipment 15 is stated to connect；
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 13, the up liquid phase
The outlet of hydrogenation reactor 14 is connected with the high pressure knockout drum 8；
There is n respectively in the descending liquid phase hydrogenation reactor 13 and the up liquid phase hydrogenation reactor 14
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 4 has 2n roads hydrogen feed pipe road, wherein 2 road hydrogen feed pipe roads and institute
State air-fuel mixture equipment be connected, remaining 2n-2 roads hydrogen feed pipe road respectively with the molten hydrogen disperser of the micropore
Connect one to one, n is integer, in the present embodiment, n is 2；Certainly, n in other embodiments
Can also be 3 or 4 or 5；
The liquid-phase hydrogenatin device also include circulating pump 12, for using reaction effluent as recycle oil with
Feedstock oil mixes, and because the raw material for processing is for hydrogen high consumes raw material, therefore the liquid-phase hydrogenatin reaction system is also included
The recycle oil pipeline 5 being connected with raw material oil-in 1, high pressure knockout drum 8 passes through circulating pump 12 and recycle oil
Pipeline is connected.
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.
The liquid phase hydrogenating method that the present embodiment is also provided, the liquid phase hydrogenating method is filled using above-mentioned liquid-phase hydrogenatin
Put, comprise the following steps：
Mix being mixed to form through the first air-fuel mixture equipment with hydrogen by the straight-run diesel oil of heating furnace
Raw material, certainly in other embodiments, it can be catalytic diesel oil and hydrogen are through the first air-fuel mixture equipment
It is mixed to form 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 separates rear portion and is mixed as recycle oil and feedstock oil through the high pressure knockout drum
Close, another part reaction effluent carries out isolated product oil, the tail gas for obtaining enters also into desulphurization plant
Row 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, and
Pass through second oil gas between the descending liquid phase hydrogenation reactor and the up liquid phase hydrogenation reactor
Mixing apparatus is connected；
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；
The liquid-phase hydrogenatin device also includes circulating pump, for using reaction effluent as recycle oil and raw material
Oil mixing.
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 hydrogen high 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 separates rear portion and is mixed as recycle oil and feedstock oil through the high pressure knockout drum
Close, another part reaction effluent carries out isolated product oil.
7. liquid phase hydrogenating method according to claim 6, it is characterised in that the hydrogen consumption raw material high
Oil is straight-run diesel oil or catalytic diesel oil.
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 |
|---|---|---|---|
| CN201510794632.4A CN106701179B (en) | 2015-11-18 | 2015-11-18 | Liquid-phase hydrogenatin device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510794632.4A CN106701179B (en) | 2015-11-18 | 2015-11-18 | Liquid-phase hydrogenatin device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106701179A true CN106701179A (en) | 2017-05-24 |
| CN106701179B CN106701179B (en) | 2018-09-04 |
Family
ID=58932678
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510794632.4A Active CN106701179B (en) | 2015-11-18 | 2015-11-18 | Liquid-phase hydrogenatin device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106701179B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| WO2020186644A1 (en) * | 2019-03-15 | 2020-09-24 | 南京延长反应技术研究院有限公司 | Downward fixed-bed enhanced reaction system with oil hydrogenation micro interface |
| WO2020186642A1 (en) * | 2019-03-15 | 2020-09-24 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening reaction system and method for preparing ship fuel by means of heavy oil hydrogenation |
| CN112705119A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reactor and hydrogenation method |
| EP4183480A4 (en) * | 2020-07-16 | 2024-04-03 | Nanjing Yanchang Reaction Technology Research Institute Co., Ltd | Micro-interface reaction system and method for diesel hydrogenation |
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 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 |
-
2015
- 2015-11-18 CN CN201510794632.4A patent/CN106701179B/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 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 |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| WO2020186644A1 (en) * | 2019-03-15 | 2020-09-24 | 南京延长反应技术研究院有限公司 | Downward fixed-bed enhanced reaction system with oil hydrogenation micro interface |
| WO2020186642A1 (en) * | 2019-03-15 | 2020-09-24 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening reaction system and method for preparing ship fuel by means of heavy oil hydrogenation |
| CN112705119A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reactor and hydrogenation method |
| 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 |
| EP4183480A4 (en) * | 2020-07-16 | 2024-04-03 | Nanjing Yanchang Reaction Technology Research Institute Co., Ltd | Micro-interface reaction system and method for diesel hydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106701179B (en) | 2018-09-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106701179A (en) | Liquid phase hydrogenation device and method | |
| CN105647577B (en) | A kind of hydro carbons Continuous Liquid Phase hydrogenation method and its device | |
| CN104560132A (en) | Method for hydrotreatment of continuous liquid-phase wax oil | |
| CN108485701B (en) | Method for hydrorefining membrane dispersion liquid phase circulation | |
| CN102049220A (en) | Method for enhancing gas-liquid mass transfer of ebullated bed hydrogenation reactor | |
| CN111068589B (en) | Liquid-phase hydrogenation system and liquid-phase hydrogenation method | |
| CN101787305B (en) | Method of liquid phase circulation hydrotreatment and reaction system | |
| CN102642911A (en) | Advanced oxidation treatment device and advanced oxidation treatment process of refractory organic wastewater | |
| WO2014117309A1 (en) | Liquid-phase hydrogenation reaction method for multi-stage hydrogen dissolution | |
| CN102311761B (en) | Low hydrogen-oil ratio hydrotreating method and reactor | |
| CN103965953B (en) | Distillate oil two-phase hydrogenation reactor and hydrogenation process | |
| CN106701174A (en) | Liquid phase hydrogenation device and method | |
| CN106701180A (en) | Liquid phase hydrogenation device and method | |
| CN206253030U (en) | A kind of feedstock oil mixing and emulsifying device | |
| CN103773441B (en) | A kind of ebullated bed liquid-phase hydrogenatin treatment process | |
| CN107880927A (en) | A kind of heavy oil plasma hydroprocessing technique and system | |
| CN112705117B (en) | Liquid phase hydrogenation reactor and hydrogenation process | |
| CN111068588B (en) | Diesel oil ultra-deep desulfurization device and diesel oil hydrogenation reaction system | |
| CN104326856B (en) | A kind of cyclopentadiene hydrogenating produces Pentamethylene. or the method for methyl cyclopentadiene hydrogenation production methyl cyclopentane | |
| CN109679689A (en) | A kind of liquid phase hydrogenation reactor and process for selective hydrogenation and reaction system | |
| CN105713659A (en) | Hydrocarbon continuous liquid-phase hydrogenation process | |
| CN106701173A (en) | Liquid-phase hydrogenation device and method | |
| CN105524657B (en) | A kind of fraction oil boiling bed hydrogenation method | |
| CN114437809B (en) | Liquid phase hydrogenation device and liquid phase hydrogenation method | |
| CN105542842A (en) | Liquid phase hydrogenation reaction apparatus, system thereof, and continuous liquid phase hydrogenation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |