CN1242409A - Process for hydro-refining/hydrogen refining petroleum fractions - Google Patents
Process for hydro-refining/hydrogen refining petroleum fractions Download PDFInfo
- Publication number
- CN1242409A CN1242409A CN99107939A CN99107939A CN1242409A CN 1242409 A CN1242409 A CN 1242409A CN 99107939 A CN99107939 A CN 99107939A CN 99107939 A CN99107939 A CN 99107939A CN 1242409 A CN1242409 A CN 1242409A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- gas
- tower
- technology
- conversion zone
- 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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The hydrofining process of petroleum fraction is characterized by that the petroleum fraction and hydrogen gas are respectively come into the column interior from top and lower portion of catalystic stripping/gas stripping column, both are counter-current-wise contacted on the surface of catalyst, and the product prouced by above-mentioned reaction is come out from the top of the column under the action of gas stripping of hydrogen gas or steam produced by reboiler, the passed through condenser and return tank, and discharged from said equipment, and the refined petroleum fraction is discharged from the bottom of the column. Said invention can simultaneously implement catalytic reaction and stripping separation in one column, and can obtain good denitrification and desulfurization effect.
Description
The invention belongs to a kind of hydrogen/hydrofining technology that faces, more particularly, is petroleum fractions and hydrogen counter current contact in catalytic distillation tower, reacts the technology of carrying out desulfurization and denitrogenation at catalyst surface.
Along with China to the requirement on environmental protection increasingly stringent, the in addition strict restriction of the sulphur in the petroleum fractions, nitrogen content.And the quality aggregate level of oil products such as the current gasoline of China, kerosene is lower, and variation along with stock oil character, the raising of the level of crude oil processing, particularly the scale of processing import crude oil constantly enlarges, kind increases, sulphur, nitrogen content rise, make sulphur in the oil product, nitrogen content increase, product quality problem is more serious.Therefore, quicken the exploitation of desulfurizing oil and denitride technology, it is very necessary to improve oil quality.
The existence form of sulphur is mainly mercaptan in the oil product, and mercaptan removal (being also referred to as deodorization) method can reduce four types: 1. extracting deodorization; 2. oxidation deodorizing; 3. deodour by adsorber; 4. extracting-oxidation deodorizing.Above-mentioned four kinds of methods all are non-hydrogen mercaptan removal methods, though investment cost is lower, and all environmental pollutions of various degrees, and indexs such as the colourity of oil product, total sulfur, smoke point are not all had improvement.
Adopt conventional trickle bed hydrogenation technique, though can reach the purpose of desulfurization and denitrogenation, indexs such as colourity, total sulfur, smoke point also all have greatly improved, and the investment and the process cost of this technology are higher.
Catalytic distillation technology (Catalytic-Distillation Technology) is a kind of novel technique that catalyzed reaction is combined and carries out simultaneously in a tower with the product fractionation.Catalyzer is contained in the stage casing of tower, and the tower upper and lower is respectively rectifying section and stripping section.Because reaction product gone out by fractionation at any time, help improving reaction conversion ratio, and will react generation heat and be directly used in distillation, but thereby conserve energy.Catalytic distillation technology is used to produce methyl tertiary butyl ether (MTBE) at first, now has been generalized to technological processs such as dimerization C 4 olefin, hydrogenation.
USP5,597, a kind of desulfurization process of gasoline is disclosed in 476, this technology is to be raw material with the pressure naphtha, the conversion zone of this tower is steamed in the lighting end that will contain most of alkene and mercaptan in first catalytic distillation tower, and mercaptan and olefine reaction generate sulfide, enter second catalytic distillation tower with the higher sulfide of boiling point at the bottom of the tower, the hydrogen feed mouth is converted into hydrogen sulfide stripping with sulfide on sulfide.
CN1189183A and USP5,779,883 disclose a kind of catalytic distillation method of hydrogenating desulfurization, this method is a raw material with petroleum naphtha, kerosene or diesel oil, with zirconium-molybdenum, nickel-molybdenum or nickel-tungsten is the activity of such catalysts component, react in the catalytic distillation tower of routine, reaction conditions is: hydrogen partial pressure 0.01～70psi (about 0～0.48MPa), temperature 400～800 (promptly 204～427 ℃), volume space velocity 0.1～10 hour
-1, hydrogen and stock oil ratio 300～3000SCFB (being that volume ratio is 53.4～534).
The objective of the invention is to provide on the basis of existing technology a kind of technology of in the new catalytic distillation tower, using catalyzer and hydrogen to remove sulphur and nitrogen in the petroleum fractions.
This new catalytic distillation tower is not established rectifying section, only is made up of conversion zone and stripping section, and conversion zone is on tower top, and stripping section is in the tower bottom.In order to distinguish with conventional catalytic distillation tower, this patent is referred to as catalysis and carries and heating up in a steamer/gas stripping column.
Technology provided by the invention is: petroleum fractions and hydrogen carry from catalysis respectively heat up in a steamer/upper and lower of gas stripping column enters in the tower, the two is in the catalyst surface counter current contact, the product that reaction generates is carried under the effect at the gas of hydrogen and being transferred to the gas phase from liquid phase, gaseous phase materials is gone out through behind condenser and the return tank from cat head, hydrogen and most of gaseous product go out device, and the liquid phase material of return tank bottom returns in the tower; Liquid phase stream in the conversion zone enters in the reboiler through stripping section downwards, and the gaseous product of minimal amounts of dissolved in liquid phase stream steamed back stripping section, and the gas of the steam that produces at hydrogen and reboiler is carried under the effect and being separated from cat head; Liquid phase stream in the conversion zone also can only be carried under the effect at the gas of hydrogen gaseous product is separated from cat head without reboiler, and the petroleum fractions after making with extra care then goes out device at the bottom of tower.
Technology provided by the invention is so concrete enforcement: petroleum fractions and hydrogen carry from catalysis respectively heat up in a steamer/upper and lower of gas stripping column enters in the tower, the petroleum fractions that flows downward is with upwards mobile hydrogen is in the catalyst surface counter current contact, and reaction conditions is hydrogen partial pressure 0.1～6.0MPa (absolute pressure), 150～350 ℃ of conversion zone temperature, volume space velocity 10～30 hours
-1The product that reaction generates is carried under the effect at the gas of hydrogen and being transferred to the gas phase from liquid phase, and gaseous phase materials is gone out through behind condenser and the return tank from cat head, and hydrogen and most of gaseous product go out device, and the liquid phase material of return tank bottom returns in the tower; Liquid phase stream in the conversion zone enters in the reboiler through stripping section downwards, and the gaseous product of minimal amounts of dissolved in liquid phase stream steamed back stripping section, and the gas of the steam that produces at hydrogen and reboiler is carried under the effect and being separated from cat head; Liquid phase stream in the conversion zone also can only be carried under the effect at the gas of hydrogen gaseous product is separated from cat head without reboiler, and the petroleum fractions after making with extra care then goes out device at the bottom of tower.
Petroleum fractions raw material among the present invention is to be selected from a kind of in aviation kerosene cut, gasoline fraction, diesel oil distillate and the heavy oil, enter catalysis carry heat up in a steamer/density of hydrogen of gas stripping column is 50～100%; Enter catalysis carry heat up in a steamer/hydrogen of gas stripping column and the volume ratio (hereinafter to be referred as hydrogen-oil ratio) of petroleum fractions raw material are 1～50: 1.
Catalysis used in the present invention carry heat up in a steamer/gas stripping column only is made up of conversion zone and stripping section, conversion zone is on tower top, it highly is 5～95% of a tower height, stripping section is in the tower bottom, it highly is the poor of tower height and conversion zone height.
Catalysis carry heat up in a steamer/conversion zone of gas stripping column is equipped with the member of being made up of filler and catalyzer, the top of member is the distribution disengaging zone, can be random filler such as Raschig ring, Pall ring, saddle packing etc. in the district, also can be regular packing such as corrugated plate type, grid type, honeycomb type etc.; The bottom of member is a reaction zone, is hydrogenation catalyst such as molybdenum tungsten hydrogenation catalyst, molybdenum cobalt hydrogenation catalyst, tungsten cobalt hydrogenation catalyst, nickeliferous catalyzer etc. in the district.The relative dimension in two districts, member upper and lower can specifically be determined according to practical situation by those skilled in the art.Member can huddle, and also can put in order block.
The voidage of member is 30～95%, so member has good gas-liquid distribution performance, low pressure drop, competent place of carrying out chemical reaction can be provided, and activity of such catalysts is given full play to.
It is as follows in conjunction with the accompanying drawings petroleum fractions provided by the invention to be faced hydrogen/hydrofining technology process description:
Carry in the catalysis that constitutes by conversion zone and stripping section heat up in a steamer/gas stripping column 10 in, the petroleum cuts raw material enters the top of tower through pipeline 1, hydrogen enters the bottom of tower by pipeline 2, the two is counter current contact in this tower.The petroleum fractions that flows downward is reacted at catalyst surface with the mobile hydrogen that makes progress.Since this catalysis carry heat up in a steamer/carrying of gas stripping column heat up in a steamer function, adds by the gas of the hydrogen that enters at the bottom of the tower and propose effect, the gaseous product that reaction produces can be transferred to the gas phase from liquid phase.Gaseous phase materials enters condenser 4 through pipeline 3.The material that is cooled enters return tank 7 through pipeline 5, and material is divided into gas-liquid two-phase in return tank.By caterpillar, liquid phase material all refluxes through pipeline 8 and enters catalysis and carry and heating up in a steamer/gas stripping column through pipeline 6 for hydrogen and most of gaseous product of being removed.Refining back petroleum cuts flows into reboilers 13 through stripping section, pipeline 9 downwards, in the process of flowing downward, is dissolved in the gaseous product in the petroleum fractions because the gas of the hydrogen that enters at the bottom of the tower is carried most of the transferring to the gas phase from liquid phase of effect is pulled away.A spot of gaseous product enters reboiler with liquid through pipeline 12, is steamed back stripping section in reboiler, carries under the effect at the gas of the steam of hydrogen and reboiler generation and separating from cat head; Liquid phase stream in the conversion zone also can only be carried under the effect at the gas of hydrogen gaseous product is separated from cat head without reboiler.Petroleum cuts after refining as product through pipeline 11 caterpillars.
When stock oil is aviation kerosene, must establish reboiler for the flash-point that guarantees product, other stock oil can not established reboiler.
The invention has the advantages that: catalyzed reaction and carrying is heated up in a steamer and is separated in a catalysis and carries and heat up in a steamer/carry out simultaneously in the gas stripping column, set up gas in the tower and put forward function, hydrogen is reactant still not, and is that gas is recommended matter, the gaseous product that reaction generates can be taken out of from tower, be had good desulfurization and denitrification effect.Big volume space velocity can make the treatment capacity of device improve greatly simultaneously, and low hydrogen-oil ratio can be saved energy consumption.
Accompanying drawing is the schematic flow sheet that petroleum fractions is faced hydrogen/hydrofining technology.
Each numbering is described as follows in the accompanying drawing:
1,2,3,5,6,8,9,11,12 is pipeline, and 4 is condenser, and 7 is return tank, and 10 carry for catalysis and to heat up in a steamer/gas stripping column, and 13 is reboiler, and empty frame table shows that reboiler can not establish among the figure.
The following examples will give further instruction to technology provided by the invention, but not thereby limiting the invention.
The main character of employed petroleum fractions raw material sees Table 1 among the embodiment, and the concentration of hydrogen is 75%.Catalysis is carried and being heated up in a steamer/1700 millimeters of gas stripping column height overalls, and wherein the conversion zone height is 1200 millimeters, and the stripping section height is 500 millimeters, and the tower internal diameter is 32 millimeters, and loaded catalyst is 65 grams.Catalysis carry heat up in a steamer/voidage that gas is carried member is 55%, the used filler of member is a Pall ring, used catalyzer is the hydrotreating catalyst that contains molybdenum or tungsten, its concrete preparation method carries out for the method that 98100765.1 patent application provides by application number.Reaction conditions among the embodiment and test-results see Table 2, table 3 and table 4.
Aviation kerosene cut and hydrogen carried from catalysis respectively in 1: 30 by volume heat up in a steamer/upper and lower of gas stripping column enters in the tower, carry out counter current contact, the petroleum fractions that flows downward is reacted at catalyst surface with the mobile hydrogen that makes progress, and reaction conditions is hydrogen partial pressure 0.6MPa (absolute pressure), 245 ℃ of temperature of reaction, volume space velocity 10.5 hours
-1The gas that reaction generates is carried under the effect at the gas of hydrogen and being transferred to the gas phase from liquid phase, and gaseous phase materials is gone out through behind condenser and the return tank from cat head, and hydrogen and most of gaseous product go out device, and the liquid phase material of return tank bottom returns in the tower; Liquid phase stream in the conversion zone enters in the reboiler through stripping section downwards, and the gaseous product of minimal amounts of dissolved in liquid phase stream steamed, and returns stripping section, carries under the effect at the gas of hydrogen, separates from cat head.Refining back aviation kerosene cut goes out device at the bottom of tower, its mercaptans content is 8ppm.
With the aviation kerosene cut is raw material, and hydrogen-oil ratio is 22: 1, and reaction conditions is hydrogen partial pressure 0.4MPa (absolute pressure), 245 ℃ of temperature of reaction, volume space velocity 12.5 hours
-1, other is all identical with embodiment 1.The mercaptans content of refining back aviation kerosene cut is 16ppm.
With the aviation kerosene cut is raw material, and hydrogen-oil ratio is 45: 1, and reaction conditions is hydrogen partial pressure 0.4MPa (absolute pressure), 308 ℃ of temperature of reaction, volume space velocity 25 hours
-1, other is all identical with embodiment 1.The mercaptans content of refining back aviation kerosene cut is 18ppm.
With the gasoline fraction is raw material, and hydrogen-oil ratio is 15: 1, and reaction conditions is hydrogen partial pressure 2.6MPa (absolute pressure), 325 ℃ of temperature of reaction, volume space velocity 18 hours
-1, with the downward modulation of gasoline fraction feed entrance point, other is all identical with embodiment 1 simultaneously.The total sulfur of refining after cut and total nitrogen content are all less than 0.5ppm.
With the diesel oil distillate is raw material, and hydrogen-oil ratio is 45: 1, and reaction conditions is hydrogen partial pressure 5.6MPa (absolute pressure), 350 ℃ of temperature of reaction, volume space velocity 16 hours
-1, other is all identical with embodiment 1.The total sulfur of refining after cut and total nitrogen content are all less than 0.5ppm, and bromine number is 0.1gBr/100g.
With the gasoline fraction is raw material, and hydrogen-oil ratio is 40: 1, and reaction conditions is hydrogen partial pressure 0.5MPa (absolute pressure), 350 ℃ of temperature of reaction, volume space velocity 16 hours
-1, other is all identical with embodiment 1.The total sulfur of refining back gasoline fraction and total nitrogen content are all less than 0.5ppm.
With the gasoline fraction is raw material, and hydrogen-oil ratio is 30: 1, and reaction conditions is hydrogen partial pressure 3.0MPa (absolute pressure), 350 ℃ of temperature of reaction, volume space velocity 25 hours
-1, other is all identical with embodiment 1.The total sulfur of refining back gasoline fraction and total nitrogen content are all less than 0.5ppm.
Table 1
| Raw material | Aviation kerosene | Gasoline | Diesel oil |
| Density, gram per centimeter
3Mercaptans content, the ppm total sulfur content, the ppm total nitrogen content, the ppm bromine number, gBr/100g boiling range (ASTM-D86), ℃ | ??0.7969 ????105 ????1255 ????- ????- ????140 ????152 ????177 ????215 ????234 | ????0.7182 ????- ????239 ????1.0 ????2.8 ????63 ????81 ????99 ????119 ????158 | ????0.8017 ????110 ????4000 ????3.6 ????- ????203 ????215 ????248 ????272 ????306 |
Table 2
| | Embodiment | 1 | | |
| Raw material reaction condition hydrogen partial pressure (absolute pressure), the MPa temperature of reaction, ℃ volume space velocity, hour -1The refining back of hydrogen-oil ratio aviation kerosene mercaptan, ppm | Aviation kerosene 0.6 245 10.5 30: 18 | Aviation kerosene 0.4 245 12.5 22: 1 16 | Aviation kerosene 0.4 308 25 45: 1 18 |
Table 3
| | Embodiment | 4 | |
| Raw material reaction condition hydrogen partial pressure (absolute pressure), the MPa temperature of reaction, ℃ volume space velocity, hour -1The refining back of hydrogen-oil ratio product main character total sulfur, the ppm total nitrogen, ppm | Gasoline 2.6 325 18 15: 1＜0.5＜0.5 | Diesel oil 5.6 350 16 45: 1＜0.5＜0.5 |
Table 4
| | Embodiment | 6 | |
| Raw material reaction condition hydrogen partial pressure (absolute pressure), the MPa temperature of reaction, ℃ volume space velocity, hour -1The refining back of hydrogen-oil ratio gasoline main character total sulfur, the ppm total nitrogen, ppm | Gasoline 0.5 350 16 40: 1＜0.5＜0.5 | Gasoline 3.0 350 25 30: 1＜0.5＜0.5 |
Claims (9)
1, a kind of petroleum fractions is faced hydrogen/hydrofining technology, it is characterized in that petroleum fractions and hydrogen carry from catalysis respectively heat up in a steamer/upper and lower of gas stripping column enters in the tower, the two is in the catalyst surface counter current contact, the gaseous product that reaction generates is carried under the effect at the gas of the steam of hydrogen or reboiler generation and being transferred to the gas phase from liquid phase, gaseous phase materials is gone out through behind condenser and the return tank from cat head, hydrogen and most of gaseous product go out device, and the liquid phase material of return tank bottom returns in the tower; Liquid phase stream in the conversion zone enters in the reboiler through stripping section downwards, and the gaseous product of minimal amounts of dissolved in liquid phase stream steamed back stripping section, and the gas of the steam that produces at hydrogen and reboiler is carried under the effect and being separated from cat head; Liquid phase stream in the conversion zone also can only be carried under the effect at the gas of hydrogen gaseous product is separated from cat head without reboiler.Petroleum fractions after refining then goes out device at the bottom of tower.
2,, it is characterized in that described petroleum fractions is to be selected from a kind of in aviation kerosene cut, gasoline fraction, diesel oil distillate and the heavy oil according to the technology of claim 1.
3, according to the technology of claim 1, it is characterized in that entering catalysis carry heat up in a steamer/density of hydrogen of gas stripping column is 50～100%.
4, according to the technology of claim 1, it is characterized in that entering catalysis carry heat up in a steamer/hydrogen of gas stripping column and the volume ratio of petroleum fractions are 1～50: 1.
5, according to the technology of claim 1, it is characterized in that described catalysis carry heat up in a steamer/gas stripping column only is made up of conversion zone and stripping section, conversion zone is on tower top, it highly is 5～95% of a tower height, stripping section is in the tower bottom, it highly is the poor of tower height and conversion zone height.
6, according to the technology of claim 1 or 5, it is characterized in that described catalysis carry heat up in a steamer/conversion zone of gas stripping column is equipped with the member of being made up of filler and catalyzer, member can huddle, and also can put in order block, the voidage of member is 30～95%.
7, according to the technology of claim 6, it is characterized in that filler can be random filler in the described member, also can be regular packing.
8,, it is characterized in that catalyzer is a hydrogenation catalyst in the described member according to the technology of claim 6.
9,, it is characterized in that described reaction conditions is hydrogen partial pressure 0.1～6.0MPa (absolute pressure), 150～350 ℃ of conversion zone temperature, volume space velocity 10～30 hours according to the technology of claim 1
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99107939A CN1076753C (en) | 1998-06-25 | 1999-06-04 | Process for hydro-refining/hydrogen refining petroleum fractions |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98102727 | 1998-06-25 | ||
| CN98102727.X | 1998-06-25 | ||
| CN99107939A CN1076753C (en) | 1998-06-25 | 1999-06-04 | Process for hydro-refining/hydrogen refining petroleum fractions |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1242409A true CN1242409A (en) | 2000-01-26 |
| CN1076753C CN1076753C (en) | 2001-12-26 |
Family
ID=25744625
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99107939A Expired - Fee Related CN1076753C (en) | 1998-06-25 | 1999-06-04 | Process for hydro-refining/hydrogen refining petroleum fractions |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1076753C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456606B (en) * | 2008-12-17 | 2011-04-06 | 天津大学 | Technique and apparatus for implementing fat phase and aqueous phase separation for wastewater by stripping method |
| CN101942318B (en) * | 2009-07-09 | 2013-10-09 | 中国石油化工股份有限公司 | Hydrocarbon two-phase hydrotreating method |
| CN103468309A (en) * | 2012-06-07 | 2013-12-25 | 中国石油化工股份有限公司 | Low sulfur gasoline production method |
| CN103627427A (en) * | 2012-08-22 | 2014-03-12 | 中国石油化工集团公司 | Two-stage hydrogenation system, and hydrogenation method |
| WO2019165065A1 (en) * | 2018-02-21 | 2019-08-29 | Cargill, Incorporated | Edible oil refining |
| CN115785993A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
| CN115785995A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Inferior diesel oil hydrotreating method and device |
| CN115785993B (en) * | 2021-09-10 | 2024-05-31 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5779883A (en) * | 1995-07-10 | 1998-07-14 | Catalytic Distillation Technologies | Hydrodesulfurization process utilizing a distillation column realtor |
| ES2214544T3 (en) * | 1995-07-10 | 2004-09-16 | CHEMICAL RESEARCH & LICENSING COMPANY | HYDRODESULFURATION PROCEDURE. |
| US5597476A (en) * | 1995-08-28 | 1997-01-28 | Chemical Research & Licensing Company | Gasoline desulfurization process |
-
1999
- 1999-06-04 CN CN99107939A patent/CN1076753C/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456606B (en) * | 2008-12-17 | 2011-04-06 | 天津大学 | Technique and apparatus for implementing fat phase and aqueous phase separation for wastewater by stripping method |
| CN101942318B (en) * | 2009-07-09 | 2013-10-09 | 中国石油化工股份有限公司 | Hydrocarbon two-phase hydrotreating method |
| CN103468309A (en) * | 2012-06-07 | 2013-12-25 | 中国石油化工股份有限公司 | Low sulfur gasoline production method |
| CN103468309B (en) * | 2012-06-07 | 2015-08-26 | 中国石油化工股份有限公司 | A kind of method of producing low-sulphur oil |
| CN103627427A (en) * | 2012-08-22 | 2014-03-12 | 中国石油化工集团公司 | Two-stage hydrogenation system, and hydrogenation method |
| CN103627427B (en) * | 2012-08-22 | 2015-07-15 | 中国石油化工集团公司 | Two-stage hydrogenation system, and hydrogenation method |
| WO2019165065A1 (en) * | 2018-02-21 | 2019-08-29 | Cargill, Incorporated | Edible oil refining |
| CN111902522A (en) * | 2018-02-21 | 2020-11-06 | 嘉吉公司 | Refining of edible oil |
| US20210071103A1 (en) * | 2018-02-21 | 2021-03-11 | Cargill, Incorporated | Edible oil refining |
| CN115785993A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
| CN115785995A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Inferior diesel oil hydrotreating method and device |
| CN115785993B (en) * | 2021-09-10 | 2024-05-31 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1076753C (en) | 2001-12-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1063352C (en) | Multi-purpose catalytic distillation column and etherification process using same | |
| RU2389754C2 (en) | Method for obtaining petroleum with low content of sulphur and alkenes | |
| CN102212394B (en) | Fluid catalytic cracking (FCC) gasoline modification method comprising light gasoline etherification process | |
| GB1602639A (en) | Process for hydrodesulphurization of heavy hydrocarbon oils | |
| CN1187523A (en) | Heavy hydrocarbon fraction converting process relating to hydrogenation demetalization in catalyst bubbling bed | |
| CN101270301A (en) | Light gasoline etherification technique and catalytically cracked gasoline modification method containing the technique | |
| KR20010034022A (en) | Hydroprocessing reactor and process having staged reaction zones | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN102337153B (en) | Hydrotreatment method of gasoline distillate oil | |
| CN102041092B (en) | Method for widening catalytic reforming feedstock | |
| CN1076753C (en) | Process for hydro-refining/hydrogen refining petroleum fractions | |
| CN102226103A (en) | Method for producing gasoline and diesel by utilizing plastic oil | |
| CN101942330A (en) | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil | |
| CN101294108B (en) | Combination method of catalytic cracking production separation and hydrogen refining | |
| CN106147839A (en) | A kind of method reducing content of sulfur in gasoline | |
| CN1912062A (en) | Hydrogenation method for producing catalytic reforming raw material | |
| EP1190017A1 (en) | Process for the desulfurization of a diesel fraction | |
| CN1472284A (en) | Method for separating and refining etherification material from catalytic cracking gasoline | |
| CN102443432A (en) | Method for producing low-sulfur gasoline by non-hydroforming sulfur and alcohol removal | |
| CN101993725B (en) | Method for producing low-sulfur gasoline | |
| CN1175090C (en) | Method for producing the clean diean diesel oil with low sulfur and low arene | |
| CN1187526A (en) | Petroleum residue catalyzing converting process relating to catalyst fixed bed hydrogenation demetalization | |
| CN101108983B (en) | Gasoline hydrodesulfurization method | |
| CN1204946C (en) | Apparatus and process for hydrogenations | |
| CN103059955B (en) | Method for producing clean gasoline from catalytic cracking gasoline |
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 | ||
| C56 | Change in the name or address of the patentee |
Owner name: CHINA PETROCHEMICAL CORPORATION; CHINA PETROCHEMIC Free format text: FORMER NAME OR ADDRESS: CHINA PETROCHEMICAL CORPORATION; CHINA PETROLEUM + CHEMICAL CORPORATION, PETROLEUM CHEMICAL ENGINEERING INSTITUTE |
|
| CP01 | Change in the name or title of a patent holder |
Patentee after: China Petrochemical Group Corp. Patentee after: Sinopec Research Institute of Petroleum Processing Patentee before: China Petrochemical Group Corp. Patentee before: Chinese petrochemical industry Research Institute of Petro-Chemical Engineering of group company |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20011226 Termination date: 20180604 |