CN102311791A - Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer - Google Patents
Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer Download PDFInfo
- Publication number
- CN102311791A CN102311791A CN2010102220775A CN201010222077A CN102311791A CN 102311791 A CN102311791 A CN 102311791A CN 2010102220775 A CN2010102220775 A CN 2010102220775A CN 201010222077 A CN201010222077 A CN 201010222077A CN 102311791 A CN102311791 A CN 102311791A
- Authority
- CN
- China
- Prior art keywords
- liquid
- gas
- hydrogen
- storage equipment
- hydrogen storage
- 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
Images
Abstract
The invention discloses a liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer. The process flow adopted by the method comprises: part of hydrogenation circulating oil and a fresh raw material are mixed to form a liquid-phase mixed material to be filled into supergravity gas-liquid hydrogen dissolution equipment together with hydrogen; through the drive of the high-speed rotation of a feeding rotor, gas-liquid countercurrent full contact is formed; the mixed liquid-phase material in which hydrogen is dissolved is discharge out from the bottom of the supergravity gas-liquid hydrogen dissolution equipment and contacted with a catalyst to undergo a hydrogenation reaction, and part of a liquid phase obtained after reaction is circulated. Compared with the prior art, the method has the advantages that: the rotation of the feeding rotor in the gas-liquid hydrogen dissolution equipment forms a supergravity field, so the gas-liquid mass transfer efficiency is increased greatly, and the liquid phase material can fully dissolve hydrogen; meanwhile, gas impurities such as H2S and NH3 in a reaction system can be removed efficiently, so that the hydrodesulfurization, denitrification, aromatic saturation, cracking and other reactions are promoted.
Description
Technical field
The present invention relates to a kind of liquid phase round-robin hydroprocessing process, particularly liquid phase material and dissolve fully that hydrogen is laggard goes into the method that reactor drum carries out hydrogenation reaction.
Background technology
Conventional fixed bed hydrogenation technology is the economical and effective means that remove impurity such as sulphur, nitrogen in the raw oil.In the operation of fixed bed hydrogenation device, often adopt higher hydrogen-oil ratio and hydrogen dividing potential drop, to guarantee the catalyst runs life-span, promote hydrogenating desulfurization, denitrogenation, aromatic hydrocarbons is saturated and the carrying out of reaction such as cracking.Yet the higher hydrogen gas circulating system of pressure needs high investment cost and running cost, has increased the oil manufacture cost indirectly.If can the hydrogen flowing quantity in the hydrotreatment process be reduced and save hydrogen gas circulating system and circulating hydrogen compressor, then can reduce the production cost of clean fuel for enterprise saves facility investment.
The perfect condition of fixed-bed reactor mass transfer is: raw oil is evenly distributed on the granules of catalyst surface, and hydrogen passes in the beds space.So hydrogen need be dissolved in the raw oil, could contact with catalyzer, participate in hydrogenation reaction.That is to say when higher hydrogen pressure of fixed bed hydrogenation process using and hydrogen-oil ratio operational condition; The wherein actual amounts of hydrogen that provides is considerably beyond the required amounts of hydrogen of chemical reaction; This operator scheme only is in order to strengthen the mass transfer power of hydrogen, to guarantee the hydrogen solubility in the raw oil.The mass transfer apparatus that present alternate transmission aspect is the most general mainly is tower class (comprising a reactor drum) equipment, and like tray column and packing tower etc., these operation of equipment are all accomplished under gravity field, and flowing of liquid phase mainly is the effect that receives gravity.Because gravity acceleration g is unalterable finite value, this has also just determined the basic act of liquid-flow from macroscopic view.On the one hand, liquid phase fluid flows with thicker stream layer in the mass transfer apparatus under the gravity field, and alternate transmission area renewal frequency is low and the transmission total area is less, makes alternate transmittance process be restricted; On the other hand, improve flow state and ability strengthening transfer process that gas speed can change liquid phase fluid, but receive the influence of liquid flooding, make that the raising of gas phase velocity is also very limited.
US6881326 has introduced a kind of two-phase hydrogenation preconditioning technique.Its technological process is that fresh feed oil, turning oil and hydrogen are dissolved in hydrogen in the oil through a mixed hydrogen production device, and the less reactor drum of oil entering of dissolving hydrogen contacts with catalyzer and carries out hydrogenation reaction, deviates from the impurity in the oil.A reaction back logistics part is circulated to mixed hydrogen production device, and a part is discharged from device as product.This method is dissolved in required hydrogen in the oil before adopting raw material and turning oil to get into reactor drum in advance, can omit the recycle hydrogen system.But should technology openly not dissolve the concrete mode of hydrogen, and after dissolving hydrogen, also be provided with the waste gas tripping device in the separator that before reactor drum, is provided with.Though can remove a small amount of waste gas that influences hydrogenation reaction (mainly being the hydrogen sulfide that removes after the reaction and ammonia etc.) like this; But the waste gas separating effect is relatively poor; Make partly that also dissolved hydrogen is separated from raw oil; Cause the solubleness of hydrogen in the raw oil to descend, finally influence hydrogenation and take off the impurity effect.
Summary of the invention
To the deficiency of prior art, the present invention provides a kind of circulation hydroprocessing process of strengthening gas-liquid mass transfer.Before raw oil gets into reactor drum; Be mixed into the hypergravity gas-liquid with partial hydrogenation reaction back logistics earlier and dissolve hydrogen storage equipment, under the hypergravity condition, with the hydrogen counter current contact; Hydrogen is dissolved in the liquid phase material with oversaturated state, efficiently deviates from simultaneously the H in the logistics after the hydrogenation reaction
2S, NH
3Deng gaseous impurities.The present invention can simplify the operation course, and saves facility investment, and good hydrogenation environment can be provided.
The method of liquid phase circulation hydrotreatment that the present invention strengthens gas-liquid mass transfer comprises following content:
Turning oil and hydrogen dissolve in the hydrogen storage equipment in the hypergravity gas-liquid and mix counter current contact behind a, fresh feed oil and the partial reaction, dissolve hydrogen and deviate from gaseous impurities.Wherein, the hypergravity gas-liquid is dissolved hydrogen storage equipment and is adopted rotary packed bed hypergravity gas-liquid contanct equipment, dissolves the H that contains of hydrogen storage equipment through the hypergravity gas-liquid
2S, NH
3Hydrogen Deng gaseous impurities dissolves the discharge of hydrogen storage equipment top from the hypergravity gas-liquid, has fully dissolved the raw oil of hydrogen and the mixture of turning oil and has dissolved the discharge of hydrogen storage equipment bottom from the hypergravity gas-liquid;
The mixture entering hydrogenator that b, step a discharge contacts with catalyzer and carries out the solid, liquid two-phase hydrogenation reaction;
C, the reacted thing of step b effluent a part as the product discharger, and another part is circulated to the hypergravity gas-liquid and dissolves hydrogen storage equipment.
It is that gas, liquid two are operated mutually that the said hypergravity gas-liquid of step (a) is dissolved hydrogen storage equipment; Control hypergravity gas-liquid is dissolved the interior gas-phase space volume of hydrogen storage equipment and is accounted for the molten hydrogen storage equipment volumetrical 20%～90% of hypergravity gas-liquid; Be preferably 50%～80%, can control through control expellant gas amount.The outside housing that hydrogen dissolves hydrogen storage equipment by the hypergravity gas-liquid gets into; Flow out by rotating shaft cylindrical central sleeve place; Raw oil and turning oil mix the back and get into the molten hydrogen storage equipment of hypergravity gas-liquid by the rotating shaft center, and the high speed rotating drive through the filler rotor forms counter current contact with hydrogen.Because the rotation of filler rotor forms super gravity field, make the gas-to-liquid contact place produce 50～1000 times universal gravity constant, thereby greatly strengthened gas-liquid mass transfer efficient.The service temperature that the hypergravity gas-liquid is dissolved hydrogen storage equipment is controlled at 100～380 ℃, is preferably 150～330 ℃; Pressure 0.5～15.0MPa is preferably 2.5～10.0MPa; Vapour-liquid ratio (volume ratio under fresh feed and the inlet hydrogen standard state) is 1: 1～60: 1, is preferably 2.5: 1～15.0: 1.The volume ratio of circulation oil mass and fresh feed (recycle ratio) is 1: 1～10: 1, is preferably 2: 1～6: 1.
The said hydrogenator of step (b) is fixed-bed reactor.Its operational condition is: temperature of reaction is 200～420 ℃, volume space velocity 0.6～5.0h
-1, be preferably 2.0～4.0h
-1, reaction pressure is 0.5～15.0MPa, is preferably 2.5～10.0MPa.
The employed catalyzer of above-mentioned steps is that the conventional fixed bed hydrogenation in this area is handled catalyzer, wherein the activity of such catalysts metal can for nickel, cobalt, molybdenum or tungsten etc. one or more.Can comprise by weight percentage like the catalyzer composition: nickel or cobalt are 0.5%～10% (calculating by its oxide compound), and molybdenum or tungsten are 1%～30% (calculating by its oxide compound), and carrier can be aluminum oxide; Silicon oxide; Aluminium oxide-silicon oxide, titanium oxide waits one or more.Catalyzer is extrudate or sphere.The bulk density of catalyzer is 0.5～1.1g/cm
3, granules of catalyst diameter (spherical diameter or bar shaped diameter) is 0.04～1.0mm, specific surface area is 80～400m
2/ g.
The raw material that the present invention handles is the hydrocarbon raw material of boiling range any cut in 130～550 ℃ of scopes.Generally include one or more mixing of spray vapour fuel, diesel oil, catalytic cracking light cycle oil (LCO), wax tailings (CGO), light vacuum gas oil (LVGO), heavy vacuum gas oil (HVGO) etc.
Advantage of the present invention is:
1, under the condition of hypergravity; Because it is big that adverse current fluidic speed of relative movement becomes; Huge shearing stress can overcome surface tension; Make the contact area between hydrogen and liquid phase material increase, thereby cause alternate transmittance process greatly to be strengthened, hydrogen can fully be dissolved in the liquid phase material with oversaturated state.
2, in the hypergravity gas-liquid is dissolved hydrogen storage equipment, when liquid phase material fully dissolves hydrogen, remove H
2S, NH
3Efficient Deng gaseous impurities improves greatly, carries with the flash distillation of routine or gas and comparing, and impurity removal percentage obviously improves, thereby promotes reactions such as hydrogenating desulfurization, denitrogenation, aromatic hydrocarbons be saturated.
3, hydrogenating desulfurization, denitrogenation, aromatic hydrocarbons are saturated etc., and reaction all is thermopositive reaction, and bigger circulation oil mass can be taken a large amount of reaction heat out of, prevents that the reactor drum temperature rise is excessive.Carry enough hydrogen simultaneously and get into reactor drum, guarantee the quantity of the required hydrogen of reaction.
4, do not need the recycle hydrogen system.Just when dissolving hydrogen, use a spot of new hydrogen, the molten hydrogen storage equipment effluent air of hypergravity gas-liquid is removed H through separating
2S, NH
3Use Deng can continuing behind the gaseous impurities.
5, with respect to the transmission equipment such as tower under the gravity field, the hypergravity gas-liquid is dissolved hydrogen storage equipment and is had that volume is little, cost is low, the efficient advantages of higher.Because operation under certain pressure; Therefore needing control hypergravity gas-liquid to dissolve is prone in the hydrogen storage equipment be full of by liquid; Causing gas-liquid mass transfer efficient to reduce with operation energy consumption increases, and therefore controls the hypergravity gas-liquid and dissolves and have the essential condition that suitable gas-phase space is the assurance steady running in the hydrogen storage equipment.
Description of drawings
Fig. 1 is a process method schematic flow sheet of the present invention.
Among the figure: 1-fresh feed oil, the 2-fresh hydrogen, 3-contains H
2S, NH
3Deng the hydrogen of gaseous impurities, 4-hypergravity gas-liquid is dissolved hydrogen storage equipment, 5-filler rotor, and 6-fully dissolves the liquid phase material of hydrogen, and 7-fixed bed hydrogenation reactor, 8-generate oil, 9-turning oil.
Embodiment
For further setting forth concrete characteristic of the present invention, will combine accompanying drawing explanation.
In conjunction with accompanying drawing 1, a kind of technological process of the present invention is:
For further specifying scheme of the present invention and effect, enumerate following examples and comparative example:
Embodiment 1-2
Present embodiment is a kind of embodiment that hydrocarbon oil hydrogenation is handled, and the operating process synoptic diagram is with reference to accompanying drawing 1.
Adopt feedstock property to see table 1-1, catalyzer is selected the FH-UDS Hydrobon catalyst of Fushun Petrochemical Research Institute's development and production for use.The composition of FH-UDS catalyzer and quality index are seen table 1-2, and processing condition are seen table 1-3, and refined diesel oil character is seen table 1-4.Dissolving the hydrogen gas-liquid volume ratio is 5: 1.Control hypergravity gas-liquid is dissolved the interior gas-phase space volume of hydrogen storage equipment and is accounted for the molten hydrogen storage equipment volumetrical 30%～80% of hypergravity gas-liquid.
Table 1-1 raw oil character
The composition and the quality index of table 1-2 catalyzer
Table 1-3 processing condition
| | Condition | 1 | |
| Temperature of reaction, ℃ | 362 | 362 | |
| Reaction pressure, MPa | 6.0 | 6.0 | |
| Circulation volume ratio (turning oil: fresh feed) | 3∶1 | 6∶1 | |
| Volume space velocity, h -1 | 3.2 | 3.2 | |
| Mix hydrogen amount/inlet amount (wt%) | 0.72 | 0.72 |
Table 1-4 treated oil character
Comparative example
Compare with embodiment, adopt common fillers tower (gas-liquid counter current contact) as dissolving hydrogen storage equipment, processing condition are seen table 2-1, and refined diesel oil character is seen table 2-2.
Table 2-1 processing condition
Table 2-2 treated oil character
Above result can find out; Adopt the contact area between hydrogen of the present invention and liquid phase material to increase, cause alternate transmittance process greatly to be strengthened, hydrogen can fully be dissolved in the liquid phase material with oversaturated state; Simultaneously the effective gas of impurity such as hydrogen sulfide and ammonia is proposed discharge; Make the hydrogenation reaction performance obviously improve, improve 30 percentage points, obtained beyond thought technique effect like desulfurization degree.
Claims (6)
1. method of liquid phase circulation hydrotreatment of strengthening gas-liquid mass transfer is characterized in that comprising following content:
Turning oil and hydrogen dissolve in the hydrogen storage equipment in the hypergravity gas-liquid and mix counter current contact behind a, fresh feed oil and the partial reaction, dissolve hydrogen and deviate from gaseous impurities;
The mixture entering hydrogenator that b, step a discharge contacts with catalyzer and carries out the solid, liquid two-phase hydrogenation reaction;
C, the reacted thing of step b effluent a part as the product discharger, and another part is circulated to the hypergravity gas-liquid and dissolves hydrogen storage equipment.
2. according to the described method of claim 1, it is characterized in that: the hypergravity gas-liquid is dissolved hydrogen storage equipment and is adopted rotary packed bed hypergravity gas-liquid contanct equipment.
3. according to claim 1 or 2 described methods, it is characterized in that: the H that contains that dissolves hydrogen storage equipment through the hypergravity gas-liquid
2S, NH
3The hydrogen of gaseous impurities dissolves hydrogen storage equipment top from the hypergravity gas-liquid discharges, and has fully dissolved the raw oil of hydrogen and the mixture of turning oil and has dissolved the discharge of hydrogen storage equipment bottom from the hypergravity gas-liquid.
4. according to claim 1 or 2 described methods; It is characterized in that: it is that gas, liquid two are operated mutually that the hypergravity gas-liquid is dissolved hydrogen storage equipment; Control hypergravity gas-liquid is dissolved the interior gas-phase space volume of hydrogen storage equipment and is accounted for the molten hydrogen storage equipment volumetrical 20%～90% of hypergravity gas-liquid, controls through control expellant gas amount.
5. according to the described method of claim 1; It is characterized in that: the service temperature that the hypergravity gas-liquid is dissolved hydrogen storage equipment is controlled at 100～380 ℃; Pressure is 0.5～15.0MPa; Volume ratio under fresh feed and the inlet hydrogen standard state is 1: 1～60: 1, and the volume ratio of circulation oil mass and fresh feed is 1: 1～10: 1.
6. according to the described method of claim 1, it is characterized in that: the said hydrogenator of step (b) is fixed-bed reactor, and its operational condition is: temperature of reaction is 200～420 ℃, volume space velocity 0.6～5.0h
-1, reaction pressure is 0.5～15.0MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102220775A CN102311791B (en) | 2010-07-07 | 2010-07-07 | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102220775A CN102311791B (en) | 2010-07-07 | 2010-07-07 | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102311791A true CN102311791A (en) | 2012-01-11 |
| CN102311791B CN102311791B (en) | 2013-11-20 |
Family
ID=45425366
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102220775A Active CN102311791B (en) | 2010-07-07 | 2010-07-07 | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102311791B (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103666545A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Diesel oil hydro-refining method |
| CN103666547A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydrocarbon oil hydrogenation treatment method |
| CN103789029A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Two-phase hydrogenation combination method |
| CN107474875A (en) * | 2017-09-22 | 2017-12-15 | 北京化工大学 | A kind of method of hypergravity diesel oil and gasoline hydrofinishing |
| US9862896B2 (en) | 2012-09-21 | 2018-01-09 | China Petroleum & Chemical Corporation | Hydrocarbon oil hydrotreating method |
| US9879186B2 (en) | 2012-09-21 | 2018-01-30 | China Petroleum & Chemical Corporation | Reformate hydrotreatment method |
| CN111068589A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation system and liquid-phase hydrogenation method |
| CN115322810A (en) * | 2021-04-26 | 2022-11-11 | 中国石油天然气股份有限公司 | Heavy oil reinforced mixed hydrogen hydrogenation process, liquid phase hydrogenation reaction system and convection rotary mixer thereof |
| CN116355652A (en) * | 2021-12-28 | 2023-06-30 | 中国石油天然气股份有限公司 | Processing method and system for inferior heavy oil |
| CN116410784A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Supergravity enhanced PAO hydrofining method and device and supergravity gas mixing device |
| CN116410779A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Supergravity gas mixing device and PAO hydrofining strengthening system and method thereof |
| CN116790285A (en) * | 2022-03-15 | 2023-09-22 | 中国石油天然气股份有限公司 | Hypergravity enhanced diesel hydrofining method and device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1507940A (en) * | 2002-12-16 | 2004-06-30 | 中国石油化工股份有限公司 | Catalytic reaction method |
| US6881326B2 (en) * | 1997-06-24 | 2005-04-19 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1608715A (en) * | 2003-10-20 | 2005-04-27 | 中国石油化工股份有限公司 | Method of eliminating impurity from gas phase |
| CN101381623A (en) * | 2008-09-12 | 2009-03-11 | 中国石油化工集团公司 | Liquid-solid two-phase hydrogenation method |
-
2010
- 2010-07-07 CN CN2010102220775A patent/CN102311791B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6881326B2 (en) * | 1997-06-24 | 2005-04-19 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1507940A (en) * | 2002-12-16 | 2004-06-30 | 中国石油化工股份有限公司 | Catalytic reaction method |
| CN1608715A (en) * | 2003-10-20 | 2005-04-27 | 中国石油化工股份有限公司 | Method of eliminating impurity from gas phase |
| CN101381623A (en) * | 2008-09-12 | 2009-03-11 | 中国石油化工集团公司 | Liquid-solid two-phase hydrogenation method |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9879186B2 (en) | 2012-09-21 | 2018-01-30 | China Petroleum & Chemical Corporation | Reformate hydrotreatment method |
| CN103666547B (en) * | 2012-09-21 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of method for hydrotreating hydrocarbon oil |
| CN103666545A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Diesel oil hydro-refining method |
| CN103666545B (en) * | 2012-09-21 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of diesel oil hydrofining method |
| CN103666547A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydrocarbon oil hydrogenation treatment method |
| US9862896B2 (en) | 2012-09-21 | 2018-01-09 | China Petroleum & Chemical Corporation | Hydrocarbon oil hydrotreating method |
| CN103789029A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Two-phase hydrogenation combination method |
| CN103789029B (en) * | 2012-11-03 | 2015-06-17 | 中国石油化工股份有限公司 | Two-phase hydrogenation combination method |
| CN107474875A (en) * | 2017-09-22 | 2017-12-15 | 北京化工大学 | A kind of method of hypergravity diesel oil and gasoline hydrofinishing |
| CN111068589A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation system and liquid-phase hydrogenation method |
| CN115322810A (en) * | 2021-04-26 | 2022-11-11 | 中国石油天然气股份有限公司 | Heavy oil reinforced mixed hydrogen hydrogenation process, liquid phase hydrogenation reaction system and convection rotary mixer thereof |
| CN115322810B (en) * | 2021-04-26 | 2024-03-26 | 中国石油天然气股份有限公司 | Heavy oil enhanced hydrogen mixing hydrogenation process, liquid phase hydrogenation reaction system and convection rotary mixer thereof |
| CN116355652A (en) * | 2021-12-28 | 2023-06-30 | 中国石油天然气股份有限公司 | Processing method and system for inferior heavy oil |
| CN116410784A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Supergravity enhanced PAO hydrofining method and device and supergravity gas mixing device |
| CN116410779A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Supergravity gas mixing device and PAO hydrofining strengthening system and method thereof |
| CN116790285A (en) * | 2022-03-15 | 2023-09-22 | 中国石油天然气股份有限公司 | Hypergravity enhanced diesel hydrofining method and device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102311791B (en) | 2013-11-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102311790B (en) | Liquid phase circular hydrogenation treatment method capable of improving mixed amount of hydrogen | |
| CN102311791B (en) | Liquid-phase circulating hydrogenation treatment method capable of reinforcing gas-liquid mass transfer | |
| US8371741B2 (en) | System and process for hydrodesulfurization, hydrodenitrogenation, or hydrofinishing | |
| CN101760233B (en) | Method for hydrocracking of coked wax oil | |
| CN102039104B (en) | Reactor and liquid-phase hydrogenation processing method | |
| CN102264671A (en) | Method for efficient use of hydrogen in aromatics production from heavy aromatic oil | |
| CN102358847B (en) | Method for producing clean diesel by full liquid phase hydrogenation | |
| CN107779225A (en) | A kind of hydro-conversion system and method | |
| CN103965959A (en) | Multistage hydrogen dissolution liquid phase hydrogenation reaction method | |
| CN102041071A (en) | Hydrogenation technology for diesel | |
| CN102311761B (en) | Low hydrogen-oil ratio hydrotreating method and reactor | |
| CN108659882B (en) | Heavy oil hydrogenation method and hydrogenation system thereof | |
| CN109679689B (en) | Liquid-phase hydrogenation reactor, hydrogenation reaction method and reaction system | |
| CN102292418A (en) | Process for hydrodesulfurization, hydrodenitrogenation, hydrofinishing, or amine production | |
| CN103773441A (en) | Boiling bed liquid phase hydrogenation treatment method | |
| CN112538384B (en) | Hydrotreating-catalytic cracking combined process method for increasing yield of isobutane and light aromatic hydrocarbons | |
| CN101942318B (en) | Hydrocarbon two-phase hydrotreating method | |
| CN103865575B (en) | A kind of method of high nitrogen catalytic cracking diesel oil liquid phase circulation hydro-upgrading | |
| CN103102943B (en) | Treating method for in-depth desulphurization and dearomatization of diesel oil fraction | |
| CN103102942B (en) | Treating method for in-depth dearomatization of diesel oil fraction | |
| CN103789016B (en) | Combined distillate oil hydroprocessing method | |
| US20210171842A1 (en) | Mixed phase two-stage hydrotreating processes for enhanced desulfurization of distillates | |
| CN102465021A (en) | Combined hydrogenation process for diesel oil | |
| CN102465027A (en) | Hydrotreating method of heavy distillate oil | |
| CN104419462A (en) | Technique for producing clean diesel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |