CN103059973B - Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed - Google Patents
Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed Download PDFInfo
- Publication number
- CN103059973B CN103059973B CN201110325258.5A CN201110325258A CN103059973B CN 103059973 B CN103059973 B CN 103059973B CN 201110325258 A CN201110325258 A CN 201110325258A CN 103059973 B CN103059973 B CN 103059973B
- Authority
- CN
- China
- Prior art keywords
- coal tar
- unit
- oil
- hydrocracking
- bed
- 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.)
- Active
Links
Abstract
The invention relates to a coal tar full-fraction hydrogenation method for coupling a slurry bed and a static bed. The coal tar full-fraction hydrogenation method mainly comprises a coal tar material pretreatment unit, a slurry bed hydrocracking unit, a primary hydrogenation product fractionation unit, a static bed hydrorefining unit, and a product distilling unit, wherein the coal tar full-fraction oil is subjected to pretreatment such as dewatering and dedusting, and enters a slurry bed reactor to carry out hydrocracking reaction after being mixed and pre-heated together with a hydrocracking catalyst; the reacted primary hydrogenation product enters the static bed hydrorefining unit through a light component obtained by fractionation; the middle fraction and the catalyst return to a slurry bed hydrogenation reactor in a circulating manner; a light component returns to a tar pretreatment unit to hydrogenate in circulation after removing a part of catalyst and coke generated in a cracking manner, and the light component is rectified to obtain naphtha and diesel oil product after common hydrorefining. The method is coal tar full-fraction hydrogenation; the utilization rate of the coal tar is improved to the maximal extent; and the coking of the heavy component of the coal tar and inactivation of the catalyst are effectively delayed by the process for coupling the slurry bed and the static bed, and the production cycle is also prolonged.
Description
Technical field
The invention belongs to coal chemical technology, relating to a kind of slurry bed system and fixed bed coupling process of full fraction of coal tar hydrogenation, take particularly full fraction of coal tar as raw material, utilizes slurry bed system and fixed bed coupling hydro method to produce petrol and diesel oil.
Background technology
Coal tar is one of main products of coal hot procedure, is a kind of multi-component mixture.According to the difference of coal heat processing technique, the coal tar obtained is divided into low temperature, middle gentle coal-tar heavy oil usually.In recent years, along with the exhaustion of petroleum resources, coal tar hydrogenating is prepared clean fuel oil and is received much concern as the substitute products of petrochemical complex, and coal tar hydrogenating technological development aspect achieves obvious progress.At present, coal tar hydrogenating technology can roughly be summarized as according to its technical characterstic: coal tar hydrorefining/hydrotreating techniques, delayed coking-hydrocracking process integration technology, the fixed bed hydrogenation cracking technology of coal tar and the suspension bed/slurry bed system/boiling bed hydrogenation cracking technology of coal tar.But, take fixed bed as the hydrogen addition technology of main reactor, for raw material with the benzoline (< 370 DEG C) in coal tar, petroleum naphtha and solar oil product is obtained by hydrogenation, this type of technology coal tar utilization ratio is low, and colloid in coal tar and heteroatoms are easily in catalyst surface coking, reduce activity and the work-ing life of catalyzer.With the coal tar hydrogenating technology that suspension bed/slurry bed system/ebullated bed is main reactor, the disposable catalyzer of usual use or can more catalyst changeout online, pollutent to be eliminated in stock oil on the impact of catalyst activity, greatly expanded for hydrogenation coal tar raw material carry out source range, and improve light oil yield to greatest extent, it is the ideal reactor of the higher raw material of process pollutant load, but this type of hydrogen addition technology is based on hydrocracking, can not directly obtain the clean fuel oil meeting Standard, and product oil-proofness is poor.For improving tar resource utilization ratio to greatest extent, obtain the light oil products of high yield and good properties, large quantities of researcher is done a lot of work in improvement coal tar hydrogenation process simultaneously.
Patent CN101240193A " a kind of coal tar multistage hydrogenation treatment technique ", with the distillate of coal tar or full cut for raw material, at certain condition, weighted BMO spaces is carried out to coal tar, hydrodemetallation (HDM) reaction, deep hydrofinishing reaction is carried out successively after removing suspended particle, after resultant of reaction is separated water outlet and light constituent, enter hydrocracking reactor, then cut out gasoline fraction, diesel oil distillate and cracking tail oil through water distilling apparatus.Compared with prior art, this technique can carry out the hydrogenation of total effluent of coal tar, and coal tar raw material utilization ratio is high, simultaneously can the long period steady running of assurance device, but this multistage hydrogenation treatment technique is comparatively complicated, and input cost is high.
In patent CN101962571A " coal tar heavy fractioning suspension bed hydrocracking method and system ", the coal tar heavy fractioning oil of the difficult hydrogenation of material handling, coal tar heavy fractioning oil and catalyzer and vulcanizing agent parallel feeding, directly enter suspended-bed reactor after catalyst vulcanization and preheating and carry out hydrocracking reaction, the product after hydrogenation obtains hydrocarbon gas, gasoline fraction, diesel oil distillate and tail oil through fractionation.Reactor in this invention does not have bed, and there is not the phenomenons such as reactor bed blocking, pressure drop increase and overtemperature, is the effective ways of process coal tar heavy ends.
Patent CN1766058A " a kind of full fraction of coal tar hydroprocessing technique ", by impurity, colloid, bituminous matter and the high full fraction of coal tar of oxygen element equal size directly enter floating bed hydrogenation device, or to mix the rear floating bed hydrogenation device that directly enters with homogeneous catalyst and carry out hydrotreatment and lighting is reacted, resultant of reaction is fractionated into the tail oil of < 370 DEG C of cuts and > 370 DEG C, < 370 DEG C of cuts enter fixed-bed reactor hydrofining, product after refining cuts out gasoline and diesel oil, simultaneously the tail oil of > 370 DEG C loops back suspended-bed reactor and reacts further and change into lightweight oil.Present method can utilize various coal tar for raw material production light-weight fuel oil.
The object of the present invention is to provide a kind of method of full fraction of coal tar hydrogenation, utilize the adaptable advantage of slurry bed system material, preliminary treatment is carried out to the coal tar material of high pollution thing, high colloid, high asphalt content, from slurry bed system preliminary isocrackate out after fractionation, enter fixed bed hydrogenation to refine and directly obtain qualified petrol and diesel oil product, the maximum using utilizing the coupling of slurry bed system and fixed bed to achieve coal tar to be worth.Meanwhile, the method also have that turndown ratio is large, cycle of operation length, safety and stability, the feature such as easy to control.
Summary of the invention
The present invention relates to a kind of slurry bed system and fixed bed coupling process of full fraction of coal tar hydrogenation, it is characterized in that coal tar hydrogenating pack processing is containing following steps:
(1) at coal tar pretreatment unit, full fraction of coal tar, through dehydration, udst separation process, mixes with hydrocracking catalyst, enters next unit through preheating;
(2) at slurry bed system Hydrocracking unit, described full fraction of coal tar oil has carried out hydrocracking and has obtained just hydrogenated products under hydrocracking catalyst effect, and this process is continuously feeding, and first hydrogenated products enter fractionation unit;
(3) at first hydrogenated products fractionation unit, described just hydrogenated products are through fractionation operation, wherein light component enters fixed bed hydrogenation refined unit, middle runnings loops back paste state bed reactor together with catalyzer, still loops back tar pretreated unit circulation hydrogenation after the heavy component coke that remove portion catalyzer and cracking process produce after filtration;
(4) at fixed bed hydrogenation refined unit, the light component of described just hydrogenated products carries out hydrotreated lube base oil under Hydrobon catalyst effect, desulfurization, denitrification reaction obtain hydrogenated products;
(5) at product rectification cell, hydrogenated products enter rectifying tower, and fractionation obtains the finished product vapour, diesel oil.
Process raw material range of the present invention is wide, it is characterized in that hydrogenating materials is the full cut of coal tar, comprise coal-tar heavy oil, coal-tar middle oil, the part cut of coalite tar or full distillate oil, and the petrochemical industry such as heavy oil, residual oil byproduct, or even two or more mixture of coal tar and heavy oil, residual oil etc.This full fraction of coal tar method of hydrotreating is the coupling process of slurry bed system and fixed bed, main body is slurry bed system Hydrocracking unit and fixed bed hydrogenation refined unit, wherein slurry bed system Hydrocracking unit uses hydrocracking catalyst, and catalyzer and tar stock parallel feeding, catalyzer consists of: WO
3content is 0.5 ~ 35.0wt%, NiO content is 0.5 ~ 25.0wt%, P
2o
5content is the carrier of 0.0 ~ 5.0wt% and surplus, and carrier is γ-Al
2o
3, MCM-41 molecular sieve, ZSM-5 molecular sieve, USY molecular sieve, natural zeolite molecular sieve one or more.Slurry bed system Hydrocracking unit operators condition is: when coal tar and catalyst mix material preheating temperature are 80 ~ 300 DEG C, cracking reaction temperature is 320 ~ 450 DEG C, pressure is 8 ~ 20MPa, liquid, volume space velocity is 0.5 ~ 3.0h
-1, hydrogen to oil volume ratio is 600: 1 ~ 2000: 1.Fixed bed hydrogenation refined unit is one section of fixed-bed reactor, the hydrotreated lube base oil of hydrogenated products at the beginning of utilizing Hydrobon catalyst to carry out, desulfurization, denitrogenation processing.Hydrobon catalyst consists of: MoO
3content is 0.5 ~ 30.0wt%, CoO content is 0.5 ~ 20.0wt%, P
2o
5content is the γ-Al of 0.0 ~ 5.0wt% and surplus
2o
3carrier; Hydrofining reaction condition is: when temperature of reaction is 250 ~ 380 DEG C, pressure is 6 ~ 15MPa, liquid, volume space velocity is 0.05 ~ 2.0h
-1, hydrogen to oil volume ratio is 600: 1 ~ 2000: 1.
Slurry bed system of the present invention and fixed bed coupling hydro method, it is characterized in that the first hydrogenated products after described hydrocracking are divided into light component through first hydrogenated products fractionation unit, middle runnings and heavy component three part, light component accounts for the 15wt% ~ 50wt% of charging, and this part enters fixed bed hydrogenation refined unit; Middle runnings accounts for the 40wt% ~ 72wt% of charging, and this part loops back paste state bed reactor together with catalyzer and continues hydrocracking reaction; Heavy component accounts for the 3wt% ~ 30wt% of charging, and this part is the coke that produces of remove portion catalyzer and cracking process after filtration, and remainder squeezes into tar pretreated unit circulation hydrogenation.For keeping activity of hydrocatalyst, removal catalyst content is 5wt% ~ 20wt%, and catalyst recycling rate is 80% ~ 95%.
Slurry bed system and the fixed bed coupling process target product of full fraction of coal tar hydrogenation of the present invention are the petrol and diesel oil meeting Standard.
Accompanying drawing explanation
The slurry bed system that accompanying drawing is full fraction of coal tar hydrogenation of the present invention and fixed bed coupling process the schematic flow sheet of technique is provided.
1-coal tar; 2-raw materials pretreatment; 3-live catalyst; The pre-warm premixing of 4-; The hydrocracking of 5-slurry bed system; 6-separation column; 7-fixed bed hydrogenation is refined; 8-rectifying tower; 9-hydrogenated gasoline product; 10-hydrogenated diesel oil product; 11-middle runnings; 12-light constituent; 13-heavy constituent+catalyzer; 14-filters; 15-heavy constituent; 16-tail oil circulates; 17-fresh hydrogen; 18-hydrogen-rich gas circulates
Embodiment
Hydrogenating materials of the present invention is the full cut of coal tar, comprise coal-tar heavy oil, coal-tar middle oil, the part cut of coalite tar or full distillate oil, and the petrochemical industry such as heavy oil, residual oil byproduct, or even the mixture of coal tar and heavy oil, residual oil etc.
According to the present invention, hydrogenating materials carries out dewatering at coal tar pretreatment unit, udst separation process, requires that water-content is less than 0.5wt%.Raw material after purification mixes with hydrocracking catalyst, enters slurry bed system Hydrocracking unit through preheating.Catalyst charge accounts for 0.1% ~ 5.0% of stock oil quality, and the preheating temperature of catalyzer and stock oil compound is 80 DEG C ~ 300 DEG C.At slurry bed system Hydrocracking unit, described hydrogenating materials has carried out hydrocracking under hydrocracking catalyst effect, and this process is continuously feeding, and first hydrogenated products enter fractionation unit.Described just hydrogenated products through fractionation operation wherein light component enter fixed bed hydrogenation refined unit, middle runnings loops back paste state bed reactor together with catalyzer, still loops back feed system and continue hydrogenation after the heavy component coke that remove portion catalyzer and cracking process produce after filtration.For keeping the overall activity of hydrocracking catalyst, the heavy component fractionated out must process after filtration, the coke that remove portion catalyzer and cracking process produce, and remainder squeezes into tar pretreated unit circulation hydrogenation.Remove 5wt% ~ 20wt% that catalyst content accounts for hydrocracking catalyst total amount.The light component of the first hydrogenated products fractionated out carries out hydrotreated lube base oil under Hydrobon catalyst effect, desulfurization, denitrification reaction obtain hydrogenated products.Hydrogenated products obtain final gasoline, diesel product through rectifying tower cutting.
According to the present invention, the finished product that coal tar refines coupling process through slurry bed system hydrocracking and fixed bed hydrogenation are gasoline and diesel oil, and coal tar utilization ratio is close to 100%.
Embodiment 1
With a kind of full cut of coal-tar heavy oil for raw material, be denoted as 1# stock oil, its character is in table 1, pre-treatment is except anhydrating and mechanical impurity, mix with hydrocracking catalyst and enter paste state bed reactor, hydrocracking reaction condition lists in table 3, head product after hydrocracking enters separation column, lighting end enters back segment fixed-bed reactor and carries out hydrofining, this part cut accounts for 15wt%, middle runnings is about 65wt% and loops back paste state bed reactor continuation hydrocracking, raw material storage tank is entered after the coke that the heavy ends of about 20wt% produces in remove portion catalyzer and reaction process after filtration, the cyclic utilization rate of catalyzer is about 80%.Light ends fixed bed hydrogenation refining reaction condition lists in table 3.After hydrofining, product cuts out gasoline and diesel product through rectifying tower, and the finished product character lists in table 4.
Embodiment 2
With the mixture of the full distillate oil of the carbolic oil cut of coal-tar heavy oil and coal-tar middle oil for stock oil, be denoted as 2# stock oil, its character is in table 1, pre-treatment is except anhydrating and mechanical impurity, raw material mixes with hydrocracking catalyst and enters paste state bed reactor, hydrocracking reaction condition lists in table 3, head product after hydrocracking enters separation column, lighting end enters back segment fixed-bed reactor and carries out hydrofining, this part cut accounts for 45wt%, middle runnings is about 50wt% and loops back paste state bed reactor continuation hydrocracking, raw material storage tank is entered after the coke that the heavy ends of about 5wt% produces in remove portion catalyzer and reaction process after filtration, the cyclic utilization rate of catalyzer is about 90%.Light ends proceeds hydrogenation desulfurization and denitrogenation reaction under Hydrobon catalyst effect, and Hydrofinishing conditions lists in table 3.Product cuts out gasoline and diesel product through rectifying tower, and the finished product character lists in table 4.
Embodiment 3
With the mixture of the full distillate oil of coalite tar and residual oil for stock oil, be denoted as 3# stock oil, its character is in table 1, pre-treatment is except anhydrating and mechanical impurity, mix with hydrocracking catalyst and enter paste state bed reactor, hydrocracking reaction condition lists in table 3, head product after hydrocracking enters separation column, lighting end enters back segment fixed-bed reactor and carries out hydrofining, this part cut accounts for 30wt%, middle runnings is about 55wt% and loops back paste state bed reactor continuation hydrocracking, raw material storage tank is entered after the coke that the heavy ends of about 15wt% produces in remove portion catalyzer and reaction process after filtration, the cyclic utilization rate of catalyzer is about 85%.Hydrofining reaction condition lists in table 3.Product cuts out gasoline and diesel product through rectifying tower, and the finished product character lists in table 4.
Table 1 stock oil character
| Stock oil | 1# | 2# | 3# |
| Density/gcm -3 | 1.1187 | 0.9762 | 0.9843 |
| C，wt％ | 93.12 | 90.10 | 91.32 |
| H，wt％ | 5.12 | 5.57 | 5.47 |
| Total sulfur content, μ g/g | 5410 | 2850 | 4130 |
| Total nitrogen content, μ g/g | 9730 | 10400 | 8010 |
| Carbon residue, wt% | 26.1 | 1.86 | 13.4 |
| Mechanical impurity, wt% | 6.54 | ＜0.1 | 3.16 |
| Metal content, μ g/g | 118.3 | 94.6 | 102.5 |
| Bituminous matter, wt% | 45.2 | 15.3 | 20.3 |
Table 2 catalyst for hydrogenation composition (all in oxide dry basis, mass percent)
Table 3 Hydrogenation Experiment operating procedure condition
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| Slurry bed system hydrocracking condition | |||
| Preheating oven temperature/DEG C | 150 | 150 | 150 |
| Reaction pressure/MPa | 12 | 10 | 12 |
| Temperature of reaction/DEG C | 390 | 380 | 380 |
| Volume space velocity/h -1 | 0.5 | 0.8 | 0.5 |
| Hydrogen to oil volume ratio | 1600 | 1200 | 1600 |
| Fixed bed hydrogenation purification condition | |||
| Reaction pressure/MPa | 8 | 6 | 8 |
| Temperature of reaction/DEG C | 375 | 360 | 360 |
| Volume space velocity/h -1 | 0.5 | 0.8 | 0.5 |
| Hydrogen to oil volume ratio | 1600 | 1200 | 1600 |
Table 4 hydrogenation the finished product character
Claims (6)
1. the slurry bed system of a full fraction of coal tar hydrogenation and fixed bed coupling process, it is characterized in that full fraction of coal tar method of hydrotreating is the coupling process of slurry bed system and fixed bed, main body is slurry bed system Hydrocracking unit and fixed bed hydrogenation refined unit, target product is gasoline and diesel oil, and hydrotreatment specifically comprises following steps:
(1) at coal tar pretreatment unit, full fraction of coal tar oil, through dehydration, udst separation process, mixes with hydrocracking catalyst, enters next unit through preheating;
(2) at slurry bed system Hydrocracking unit, described full fraction of coal tar oil has carried out hydrocracking under hydrocracking catalyst effect, and this process is continuously feeding, and first hydrogenated products enter fractionation unit;
(3) at first hydrogenated products fractionation unit, described just hydrogenated products through fractionation operation wherein light component enter fixed bed hydrogenation refined unit, middle runnings loops back paste state bed reactor together with catalyzer, and heavy component is gone out after filtration after coke that partially catalyzed agent and cracking process produce and still looped back coal tar pretreatment unit circulation hydrogenation;
(4) at fixed bed hydrogenation refined unit, the light component of described just hydrogenated products carries out hydrotreated lube base oil, desulfurization, denitrification reaction under Hydrobon catalyst effect, and obtain hydrogenated products, hydrofining reactor is one section of fixed-bed reactor;
(5) at product rectification cell, hydrogenated products enter rectifying tower, carry out cut cutting and obtain the finished product vapour, diesel oil.
2. method according to claim 1, is characterized in that hydrogenating materials is the full cut of coal tar, comprises the full distillate oil of coal-tar heavy oil, coal-tar middle oil, coalite tar.
3. method according to claim 1, is characterized in that the hydrocracking catalyst that slurry bed system Hydrocracking unit uses consists of: WO
3content is 0.5 ~ 35.0wt%, NiO content is 0.5 ~ 25.0wt%, P
2o
5content is the carrier of 0.0 ~ 5.0wt% and surplus, and carrier is γ-Al
2o
3, MCM-41 molecular sieve, ZSM-5 molecular sieve, USY molecular sieve, natural zeolite molecular sieve one or more, slurry bed system Hydrocracking unit operators condition is: coal tar and catalyst mix material preheating temperature are 80 ~ 300 DEG C, cracking reaction temperature is 320 ~ 450 DEG C, pressure is 8 ~ 20MPa, catalyzer liquid time volume space velocity be 0.5 ~ 3.0h
-1, hydrogen to oil volume ratio is 600:1 ~ 2000:1.
4. method according to claim 1, after it is characterized in that described hydrocracking, product is divided into light component through first hydrogenated products fractionation unit, middle runnings and heavy component three part, light component accounts for the 15wt% ~ 50wt% of charging, and this part enters fixed bed hydrogenation refined unit; Middle runnings accounts for the 40wt% ~ 72wt% of charging, and this part loops back paste state bed reactor together with catalyzer and continues hydrocracking reaction; Heavy component accounts for the 3wt% ~ 30wt% of charging, and this part is the coke that produces of remove portion catalyzer and cracking process after filtration, and remainder squeezes into coal tar pretreatment unit circulation hydrogenation.
5. method according to claim 1, it is characterized in that described just hydrogenated products fractionation unit removal catalyst content is 5wt% ~ 20wt%, to keep catalyst activity, catalyst recycling rate is 80% ~ 95%.
6. method according to claim 1, it is characterized in that in described fixed bed hydrogenation refined unit, reactor is one section of fixed-bed reactor, Hydrobon catalyst consists of: MoO
3content is 0.5 ~ 30.0wt%, CoO content is 0.5 ~ 20.0wt%, P
2o
5content is the γ-Al of 0.0 ~ 5.0wt% and surplus
2o
3carrier; Hydrofining reaction condition is: temperature of reaction is 250 ~ 380 DEG C, pressure is 6 ~ 15MPa, catalyzer liquid time volume space velocity be 0.05 ~ 2.0h
-1, hydrogen to oil volume ratio is 600:1 ~ 2000:1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110325258.5A CN103059973B (en) | 2011-10-24 | 2011-10-24 | Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110325258.5A CN103059973B (en) | 2011-10-24 | 2011-10-24 | Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103059973A CN103059973A (en) | 2013-04-24 |
| CN103059973B true CN103059973B (en) | 2015-06-03 |
Family
ID=48102878
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110325258.5A Active CN103059973B (en) | 2011-10-24 | 2011-10-24 | Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103059973B (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103215072B (en) * | 2013-05-10 | 2015-01-07 | 成都博晟能源科技有限公司 | Method for producing diesel oil based on high-efficiency hydro-conversion of coal tar |
| CN103215070B (en) * | 2013-05-10 | 2015-02-04 | 成都博晟能源科技有限公司 | Method for producing diesel oil from coal tar |
| CN104419461B (en) * | 2013-08-19 | 2016-08-10 | 任相坤 | The slurry bed system of a kind of coal tar and fixed bed serial hydrogenation technique |
| CN104624227A (en) * | 2013-11-15 | 2015-05-20 | 中国石油天然气股份有限公司 | Mesoporous-microporous molecular sieve hydrocracking catalyst |
| CN104178209A (en) * | 2014-07-31 | 2014-12-03 | 何巨堂 | Joint hydrogenation method for different fractions of high aromatic hydrocarbons |
| CN104194828A (en) * | 2014-08-06 | 2014-12-10 | 何巨堂 | Inferior hydrocarbon hydrogenation method comprising reaction heat recycling step |
| CN104258888A (en) * | 2014-09-25 | 2015-01-07 | 中国科学院山西煤炭化学研究所 | Hydrocracking catalyst capable of reducing polycyclic aromatic hydrocarbon compounds in coal tar and application thereof |
| CN104449842B (en) * | 2014-12-03 | 2017-03-22 | 宁波市化工研究设计院有限公司 | Coal tar hydrogenation whole-fraction method |
| CN105733668B (en) * | 2014-12-06 | 2017-08-22 | 中国石油化工股份有限公司 | A kind of Hydrotreatment method for coal tar |
| CN107557064B (en) * | 2016-06-30 | 2019-12-27 | 中国石油化工股份有限公司 | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation |
| CN107557069B (en) * | 2016-06-30 | 2020-03-24 | 中国石油化工股份有限公司 | Method and system for hydro-conversion of coal tar raw material |
| CN107557068B (en) * | 2016-06-30 | 2019-12-27 | 中国石油化工股份有限公司 | Coal tar hydrogenation method and system for coal tar hydrogenation |
| CN107557065B (en) * | 2016-06-30 | 2019-12-27 | 中国石油化工股份有限公司 | Method for producing clean diesel oil by coal tar hydrogenation and system for method |
| US10563139B2 (en) * | 2016-10-28 | 2020-02-18 | Uop Llc | Flexible hydroprocessing of slurry hydrocracking products |
| CN114425428B (en) * | 2020-10-14 | 2023-10-31 | 中国石油化工股份有限公司 | Full fraction catalytic diesel hydrofining catalyst and preparation method and application thereof |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100345946C (en) * | 2004-10-29 | 2007-10-31 | 中国石油化工股份有限公司 | Coal tar whole fraction hydrotreatment process |
| CN101240193B (en) * | 2007-02-09 | 2011-06-22 | 中国石油化工股份有限公司 | Coal tar multistage hydrogenation treatment technique |
| CN101885982B (en) * | 2010-06-23 | 2013-04-10 | 煤炭科学研究总院 | Hydrogenation method for coal tar suspension bed of heterogeneous catalyst |
-
2011
- 2011-10-24 CN CN201110325258.5A patent/CN103059973B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN103059973A (en) | 2013-04-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103059973B (en) | Coal tar full-fraction hydrogenation method for coupling slurry bed and static bed | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| CN100558863C (en) | A kind of combined method of producing cleaning oil from coal-tar oil | |
| CN101724457B (en) | Hydrogenation combined method for diesel oil | |
| CN101067089A (en) | Shale oil producing process | |
| CN105647573A (en) | Method for producing light-weight aromatic hydrocarbons and clean fuel oil by moving bed hydrocracking | |
| CN101033409A (en) | Method of hydrogenation conversion for anthracene oil | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN103540352A (en) | Coal tar processing method for increasing yield of light oils | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN103602347A (en) | Hydrocracking method of high-acid high-nitrogen low-sulfur naphthenic offshore oil | |
| CN103102976B (en) | Treatment method of ethylene tar | |
| CN103059946B (en) | Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method | |
| CN103805243B (en) | A kind of method extending inferior patrol operation period of hydrogenation device | |
| CN103805253B (en) | Inferior patrol hydroprocessing process | |
| CN102796560A (en) | Coal tar whole-fraction hydrogenation method | |
| CN104277878B (en) | A kind of two-stage slurry state bed hydroprocessing technique of high temperature coal-tar | |
| CN103059951B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined technological method | |
| CN103102978B (en) | Processing method of ethylene tar | |
| CN103059956B (en) | Deep hydrodesulfurization method for catalytic gasoline | |
| CN114574239A (en) | Preparation method of marine fuel oil | |
| CN103805265B (en) | A kind of method extending inferior patrol operation period of hydrogenation device | |
| CN103805261B (en) | A kind of inferior patrol hydrodesulfurizationprocess process | |
| CN103059957B (en) | A kind of Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method | |
| CN103773430B (en) | A kind of wax oil hydrogenation treatment process |
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 |