CN103773477A - Coal tar and residuum hydrocracking-delayed coking combination processing method - Google Patents
Coal tar and residuum hydrocracking-delayed coking combination processing method Download PDFInfo
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Abstract
The invention discloses a coal tar and residuum hydrocracking-delayed coking combination processing method which is as follows: light and heavy coal tar are obtained by reduced pressure distillation of coal tar; the light coal tar is mixed with and residuum, and enters a fluidized bed reactor together with hydrogen to contact a hydrocracking catalyst for hydrocracking reaction, a hydrocracked effluent is separated to obtain a gas and a liquid phase product, gasoline, diesel, vacuum gas oil and tail oil are obtained by fractionation of the liquid phase product; the tail oil and the heavy coal tar together enter a delayed coking unit for thermal cracking reaction to obtain coker dry gas, coker gasoline, coker diesel oil, coker gas oil and coke. The process method can improve the conversion rate of raw materials, reduce coking, increase the yield of light oil, and prolong the device operation cycle, and provides a processing method for low-added-value coal tar and residuum to improve the economical efficiency.
Description
Technical field
The present invention relates to a kind of coal tar and residual oil combined treatment process method, specifically relate to a kind of coal tar and residual hydrocracking-delayed coking combined treatment process method.
Background technology
Along with global economy fast development, the demand of clean fuel oil is increasing.But at present, main force's oil field major part of main oil producing country of the world has entered the exploitation middle and later periods, crude quality is in poor quality increasingly, residual oil quality also worse and worse accordingly, how effectively to utilize these residual oil, especially poor residuum, the light oil with high yield product as far as possible of realizing, to meet growing demand, are the current important topics facing.
On the other hand, along with the conventional resource proportions such as light crude diminish, it is large that the proportion of the unconventional resource of coal tar wet goods starts to become, coal tar is the by product producing in high-temperature coking process, generally in primary distillation process, coal tar is mainly divided into following component: light oil, carbolic oil, naphtalene oil, washing oil, lightweight carbolineum, heavy carbolineum, the products such as pitch, the tar distillation technique of maturation is mainly divided into underpressure distillation both at home and abroad at present, air distillation and atmospheric and vacuum distillation, coal tar obtains different head products by above-mentioned technique, as carbolic oil, naphtalene oil etc., then refine respectively, the techniques such as extraction obtain different Chemicals, wherein a lot of compounds are plastics, synthon, dyestuff, the raw materials such as medicine, coal tar is except as industrial chemicals, and along with the shortage of petroleum resources and light-weight fuel oil demand is constantly increased, coal tar is developed gradually hydrogenation and produced light-weight fuel oil, for meeting ever-increasing light Fuel demand.But in view of China's coal tar characteristic distributions and state-of-the-art, the development of the coal tar of China exists some problems: tar source mill mostly is downstream, coke-oven plant affiliated enterprise, self tar yield limits its scale, small scale, and it is wide to distribute, and is difficult to form scale and benefit; China only using tar source mill as coking affiliated enterprise, does not set it as separately an industry and develops always; Be subject to the restriction of China's coal tar production technology, most product quality that coal tar is produced are not high, and especially pitch, is difficult to find market or can only processes at a low price.Comprehensive, the coal tar processing technology of China with there is a certain distance abroad.
Residual oil complete processing mainly comprises decarburization and hydrogenation two classes at present, decarburization mainly comprises RFCC, coking and solvent deasphalting etc., hydrogenation technique mainly comprises fixed bed hydrogenation, boiling bed hydrogenation, floating bed hydrogenation and moving-bed hydrogenation etc., wherein ripe with fixed bed hydrogenation and boiling bed hydrogenation, especially fixed bed hydrogenation technology maturation, easy and simple to handle, at present worldwide, fixed bed residual hydrogenation ability accounts for the over half of the total working ability of residual hydrogenation.Fixed bed hydrogenation is more intense to the adaptability of raw material, but still have some limitations, especially when process asphaltene or carbon residue are higher poor residuum, along with the raising of transformation efficiency, poor residuum colloidal dispersion because of asphalt content high, aromaticity diminishes etc. former thereby causes colloidal dispersion to be destroyed, unstable, in the time that transformation efficiency is lower, just there will be coking phenomenon, finally cause the coking of catalyst surface carbon distribution, both transformation efficiency and the yield of light oil of residual oil had been affected, shorten again the device operational cycle, therefore the transformation efficiency and the prolong operating period that how to improve as much as possible poor residuum are problems being badly in need of at present solution.
Patent CN101538482A discloses coalite tar deep processing way in one, described method is first to carry out fractionation after middle coalite tar pre-treatment, obtain lighting end, carbolic oil and last running, carbolic oil carries out phenol removal, obtain phenol products and dephenolize oil, dephenolize oil carries out pyrogenic reaction jointly with the last running that fractionation obtains, obtain various coking products, wherein coking naphtha, the lighting end that at least one in coker gas oil and wax tailings obtains with raw material fractionation mixes carries out hydrofining and hydrocracking reaction, the hydrotreated naphtha that hydrocracking obtains carries out catalytic reforming-Aromatics Extractive Project, obtain benzene, toluene, dimethylbenzene and solvent wet goods product.In this patent, last running except carbolic oil and light oil enters coking tower and reacts, there are the good light-end products of quality such as some naphtalene oils, carbolineum at this part heavy distillate, these light-end products, because colloid and the more coking of aromatic hydrocarbon content are easy to produce coke, reduce its potential economic worth.
Patent CN102443414A discloses a kind of heavy raw material boiling bed hydrogenation treatment method, use boiling bed hydrogenation treatment reactor, heavy raw oil and hydrogen enter reactor from bottom, under heavy raw oil hydroprocessing condition, react, reacting rear material is discharged reactor from top, in boiling bed hydrogenation treatment reactor, use the mixed catalyst of at least two kinds of catalyzer, its mixed volume is than being 1:(0.1～10).This method is that heavy raw oil enters separately ebullated bed reactor, under hydrogen and catalyzer existence condition, carry out hydrotreatment reaction, but when heavy feed stock oil nature poor especially when as high in asphalt content, in this case, heavy raw oil itself is easy to the bad stability with the raising of transformation efficiency, cause occurring the phenomenon of reaction product phase-splitting coking in follow up device, then cause device to stop up, affect the long-term operation of device.
Summary of the invention
In existing technique, low and the ropy problem of the easy coking of the independent hydrocracking of poor residuum and coal tar, low conversion rate and yield of light oil, the lightweight coal tar that the present invention obtains poor residuum and coal tar underpressure distillation is mixed and enters ebullated bed reactor and carry out hydrocracking reaction, together with the heavy coal tar fraction that hydrocracking tail oil obtains with coal tar underpressure distillation, enter coker and carry out heat cracking reaction, gained light oil yield is high, good product quality.
Coal tar of the present invention and residual hydrocracking-delayed coking combination treatment method, comprise following content:
(1) coal tar, after underpressure distillation, obtains lightweight coal tar and heavy coal tar;
(2) after the lightweight coal tar in step (1) and residual oil mix, enter ebullated bed reactor together with hydrogen, contact with hydrocracking catalyst, carry out hydrocracking reaction;
(3) step (2) gained hydrocracking effluent enters separator, separates and obtains gas and liquid product, and described liquid product enters separation column fractionation and obtains gasoline, diesel oil, vacuum gas oil and tail oil;
(4) tail oil in step (3) enters delayed coking unit with together with heavy coal tar in step (1), carries out heat cracking reaction, obtains coking dry gas, coker gasoline, coker gas oil, coker gas oil and coke.
In the inventive method, doing of lightweight coal tar described in step (1) is 480～500 ℃.
In the inventive method, step (3) gained vacuum gas oil can loop back ebullated bed reactor, is mixed and carries out hydrocracking reaction, vacuum gas oil and residual oil circulation weight ratio 0.05～0.18 with residual oil.
In the inventive method, in step (4), delayed coking gained coker gas oil can loop back boiling bed hydrogenation reactor, is mixed and carries out hydrocracking reaction with residual oil, and coker gas oil and residual oil circulation weight ratio are 0.05～0.25.
In the inventive method, the lightweight coal tar in step (1) can also enter ebullated bed reactor along reactor tangential direction from the position of one or more different heights of ebullated bed reactor beds.
In the inventive method, lightweight coal tar is 1:10～1:1 with the mixed weight ratio of residual oil raw material, preferably 1:8～1:1.
The hydrocracking catalyst adopting in the inventive method is loaded catalyst, wherein the active metal of catalyzer can be nickel, cobalt, molybdenum or tungsten etc. one or more, in metal oxide, nickel or cobalt contents are 1wt%～12wt%, and molybdenum or tungsten are 2wt%～15wt%.Granules of catalyst diameter is 0.3mm～0.8mm, and bulk density is 0.6～0.9g/cm
3, specific surface area is 100～280m
2/ g.
In the inventive method, ebullated bed reactor hydrocracking condition is: 380～450 ℃ of temperature of reaction, reaction pressure 8～20MPa, air speed 0.2～3.0h
-1, hydrogen to oil volume ratio 600～2500.Optimum condition is: 400 ℃～440 ℃ of temperature of reaction, reaction pressure 12～16MPa, air speed 0.5～1.5h
-1, hydrogen to oil volume ratio 800～1200.
In the inventive method, described delayed coking unit comprises at least one process furnace, two coke drums and a separation column, and production technique is divided into coking and decoking two portions, and coking is continous way operation, and decoking is batch operation.Delayed coking unit reaction conditions is: furnace outlet temperature is 450～525 ℃, and coke drum pressure is 0.15～0.35MPa, and recycle ratio is 0.15～0.60.
In the inventive method, described residual oil can be long residuum, vacuum residuum, high viscous crude, one or more in visbreaking residue, tar-bitumen, oil sands bitumen, ethylene cracker tar or refinery's sump oil (mud).
In the inventive method, described coal tar is the viscous liquid product of coal at high temperature carbonization and gasification byproduct in process, and productive rate accounts for 3%～5% of coking dry coal.
The separating device adopting in the inventive method comprises hot high score, low point of heat, cold high score and cold low grading, and fractionation apparatus can be atmospheric fractional tower or vacuum fractionation tower.
The inventive method tool has the following advantages:
1, when coal tar or the independent hydrogenation reaction of poor residuum, because raw material self component characteristic there will be the easy coking of system, the problems such as low conversion rate, be lightweight coal tar and heavy coal tar by coal tar fractional distillation, by lightweight coal tar and residual oil combined treatment, heavy coal tar and tail oil are mixed to the gasifying device processing that defocuses, can effectively improve aromaticity and the W(colloid+aromatic hydrocarbon of whole ebullated bed reactor material system) saturated point+bituminous matter of/W() ratio, aromaticity uprises and W(colloid+aromatic hydrocarbon) saturated point+bituminous matter of/W() ratio becomes and greatly all can improve mixed system colloidal stability and to bitum dissolving power, and then the transformation efficiency of raising raw material, reduce coking, improve yield of light oil, prolong operating period.
2, in residual oil colloidal structure, in absorption-solvated layer, some hydro carbons is subject to the additional graviational interaction of glue core, even it reaches boiling point and is also difficult to proceed to gas phase under without additional active additive effect, finally be trapped in and in condensed-nuclei aromatics, form coke, phenol in lightweight coal tar fraction is a kind of well active additive, it can make pitch micelle and glue core have an effect, weaken its additional gravitational field, the hydro carbons that is adsorbed and wraps up is released more, can improve yield of light oil on the one hand, can reduce on the other hand coke and produce.
3, in the inventive method, lightweight coal tar is taked to enter ebullated bed reactor from the position of several different heights of ebullated bed reactor beds along the tangential direction of reactor, under the condition of high temperature, adopt sectional feeding mode, two kinds of raw materials can be realized better and dissolving each other under boiling state, strengthen aromaticity and the colloidal stability of whole system.
4, in the inventive method, in vacuum gas oil, be rich in aromatic hydrocarbon, loop back ebullated bed reactor, can further improve the stability of mixing raw material system and to bitum solubleness, the coking reaction of residual oil be played to retardation.
5, the present invention, for the lower residual oil of added value and coal tar provide a kind of working method that improves its economy, under the present situation of crude supply growing tension and environmental requirement increasingly stringent, adopts this technique to reduce discharging synergy to refinery useful.
Accompanying drawing explanation
Fig. 1 is coal tar of the present invention and residual hydrocracking-delayed coking combination process schematic flow sheet.
Embodiment
As shown in Figure 1, coal tar 1, after vacuum still 2 fractionation, obtains lightweight coal tar 3 and heavy coal tar 4.After mixing, residual oil 5 and hydrogen 6 enters reactor from boiling from reactor 7 bottoms, lightweight coal tar 3 can enter ebullated bed reactor 7 along the tangential direction of reactor from the different heights position of ebullated bed reactor 7 beds, mixing raw material contacts with hydrocracking catalyst and carries out hydrocracking reaction, hydrocracking effluent 8 is after separator 9 separates, gas 10 gases are outer row after the operation such as alkali cleaning, liquid product 11 enters separation column 12, after fractionation, obtain gasoline 13, diesel oil 14, vacuum gas oil 15 and tail oil 16, wherein, vacuum gas oil 15 parts loop back ebullated bed reactor 7 as turning oil 16, remainder vacuum gas oil 17 can be used as catalytic cracking or hydrocracking raw material, after mixing, tail oil 18 and heavy coal tar 4 enters delayed coking unit 19, after reaction fractionation, obtain respectively coking dry gas 20, coker gasoline 21, coker gas oil 22, coker gas oil 23 and coke 26, wherein, a part for coker gas oil 23 loops back ebullated bed reactor 7 as the further hydrotreatment of hydrogenating materials as turning oil 24, remainder coker gas oil 25 goes out device as catalytically cracked material.
Further illustrate the present invention program below by specific embodiment, but be not limited to described embodiment.
The test feedstock property that adopts is listed in table 1, and test technology flow process is with reference to shown in Fig. 1, and reaction conditions is in table 2.Tungsten-the nickel catalyzator of ebullated bed reactor hydrocracking catalyst take aluminum oxide as carrier, wherein in catalyzer, nickeliferous 6wt%(presses NiO calculating), tungstenic 12wt%(presses WO
3calculate).Granules of catalyst diameter is 0.5mm, and bulk density is 0.79g/cm
3, specific surface area is 260m
2/ g, residual oil and coal tar character are referring to table-1.
Embodiment 1
Test to adopt doing of lightweight coal tar in raw material be 485 ℃, the ratio of residual oil and lightweight coal tar is 5:1, test technology flow process as shown in Figure 1.Tungsten-the nickel catalyzator of ebullated bed reactor hydrocracking catalyst take aluminum oxide as carrier, wherein in catalyzer, nickeliferous 6wt%(presses NiO calculating), tungstenic 12wt%(presses WO
3calculate).Granules of catalyst diameter is 0.5mm, and bulk density is 0.79g/cm
3, specific surface area is 260m
2/ g.Reaction conditions, product distribution and product property are in table 2～table 5.Vacuum gas oil and coker gas oil part loop back ebullated bed reactor, and recycle ratio is 0.1.
It is 1:1 that test adopts the ratio of residual oil and lightweight coal tar in feedstock property, and test technology flow process as shown in Figure 1.Tungsten-the nickel catalyzator of ebullated bed reactor hydrocracking catalyst take aluminum oxide as carrier, wherein in catalyzer, nickeliferous 6wt%(presses NiO calculating), tungstenic 12wt%(presses WO
3calculate).Granules of catalyst diameter is 0.5mm, and bulk density is 0.79g/cm
3, specific surface area is 260m
2/ g.Reaction conditions, product distribution and product property are in table 2～table 5.Vacuum gas oil and coker gas oil part loop back ebullated bed reactor, and recycle ratio is 0.15.
Comparative example 1
Identical with embodiment 1, different is the raw materials used residual oil that only has, and feedstock property, reaction conditions, product distribution and product property are in table 1～5.
Comparative example 2
Identical with embodiment 1, different is the raw materials used coal tar that only has, and feedstock property, reaction conditions, product distribution and product property are in table 1～5.
Table 1 residual oil and coal tar raw material character
| Project | Residual oil | Coal tar | Lightweight coal tar | Heavy coal tar |
| Density (20 ℃), g.cm -3 | 1.01 | 1.15 | 1.05 | 1.20 |
| Ultimate analysis, % | ? | ? | ? | ? |
| C | 84.27 | 89.3 | 88.43 | 90.51 |
| H | 10.4 | 6.46 | 8.15 | 3.94 |
| S | 3.31 | 0.67 | 0.76 | 0.53 |
| N | 0.5 | 0.67 | 0.78 | 0.55 |
| O | 1.52 | 2.9 | 1.88 | 4.47 |
| Carbon residue, % | 21.02 | 4.1 | 0.34 | 9.71 |
| PONA analysis, % | ? | ? | ? | ? |
| Stable hydrocarbon | 16.7 | 11.5 | 0.29 | 28.4 |
| Aromatic hydrocarbon | 45.82 | 55.0 | 70.79 | 31.3 |
| Colloid | 30.19 | 24.8 | 28.56 | 19.1 |
| Bituminous matter | 7.28 | 29.5 | 0.35 | 21.2 |
| Metal content, μ g.g-1 | ? | ? | ? | ? |
| Ni | 61.36 | 41.7 | 0.32 | 56.2 |
| V | 171.5 | 10.7 | 0.03 | 26.4 |
Table 2 hydrocracking-delay coking process condition
| Numbering | Embodiment 1 | |
Comparative example 1 | Comparative example 2 |
| Hydrocracking process condition | ? | ? | ? | ? |
| Temperature of reaction, ℃ | 410 | 425 | 410 | 425 |
| Reaction pressure, |
12 | 15 | 12 | 15 |
| Hydrogen to oil volume ratio | 400 | 800 | 400 | 800 |
| Reaction velocity, h -1 | 0.5 | 1.0 | 0.5 | 1.0 |
| Delay coking process condition | ? | ? | ? | ? |
| Furnace outlet temperature, ℃ | 495 | 500 | 495 | 500 |
| Coke drum pressure, MPa | 0.16 | 0.17 | 0.16 | 0.17 |
Table 3 hydrocracking-delayed coking product distributes
| Numbering | Embodiment 1 | |
Comparative example 1 | Comparative example 2 |
| Hydrocracking (being as the criterion with fresh feed), wt% | ? | ? | ? | ? |
| Gas | 1.7 | 1.86 | 1.6 | 2.0 |
| Gasoline | 1.6 | 1.75 | 1.5 | 1.6 |
| Diesel oil | 25.6 | 52.94 | 14.6 | 15.3 |
| Vacuum gas oil | 18.5 | 14.5 | 20.4 | 18.1 |
| Tail oil | 52.6 | 28.95 | 61.90 | 63.0 |
| Delayed coking (being as the criterion with fresh feed), wt% | ? | ? | ? | ? |
| Coking dry gas | 10.5 | 9.9 | 11.0 | 12.3 |
| Liquid is received | 59 | 66.1 | 56.2 | 53.0 |
| Coke | 30.5 | 24 | 32.8 | 34.7 |
| Add up to | 100 | 100 | 100 | 100 |
Table 4 hydrocracking product property
| Numbering | Embodiment 1 | |
Comparative example 1 | Comparative example 2 |
| Gasoline | ? | ? | ? | ? |
| Sulphur content, % | 0.15 | 0.10 | 0.23 | 0.05 |
| Octane value (RON) | 65 | 56 | 72 | 49 |
| Diesel oil | ? | ? | ? | ? |
| Cetane value | 43 | 40 | 45 | 31 |
| Sulphur, % | 1.45 | 0.44 | 1.66 | 0.1 |
| Nitrogen, % | 0.23 | 0.12 | 0.25 | 0.29 |
| Vacuum gas oil | ? | ? | ? | ? |
| Density (20 ℃)/g.cm -3 | 0.95 | 1.00 | 0.93 | 1.07 |
| Carbon residue, % | 0.03 | <0.01 | 0.05 | <0.01 |
| Tail oil | ? | ? | ? | ? |
| Density (20 ℃)/g.cm -3 | 1.11 | 1.23 | 1.09 | 1.25 |
| Carbon residue, % | 20.57 | 13.75 | 24.5 | 15 |
| （Ni+V），μg.g -1 | 108.5 | 75.6 | 185.3 | / |
| S，% | 2.09 | 1.32 | 2.4 | 0.17 |
| N，μg.g -1 | 4508 | 2637 | 6023 | 6620 |
Table 5 delayed coking product property
| Numbering | Embodiment 1 | |
Comparative example 1 | Comparative example 2 |
| Coker gasoline | ? | ? | ? | ? |
| Octane value | 56 | 53 | 60 | 48 |
| Bromine valency, g(Br)/100g | 63.5 | 60.7 | 61.2 | 58 |
| Coker gas oil | ? | ? | ? | ? |
| Cetane value | 49 | 46 | 52 | 48 |
| Bromine valency, g(Br)/100g | 51 | 42 | 40 | 41 |
| Wax tailings | ? | ? | ? | ? |
| Carbon residue, % | 0.52 | 0.45 | 0.74 | 0.86 |
| Coke | ? | ? | ? | ? |
| Ash content | 0. 30 | 0. 15 | 0. 35 | 0.20 |
| Sulphur, % | 2.6 | 2.0 | 3.5 | 0.15 |
By more known with comparative example, the liquid that adopts this inventive method can improve hydrocracking process is received yield, especially diesel yield and is obtained larger raising; In addition, in subsequent delay coking treating processes, can improve liquid and receive yield, reduce coke yield, can implement device long-term operation; And in petrol and diesel oil properties, foreign matter content keeps lower level, all in all, this inventive method can realize higher economic benefit.
Claims (13)
1. coal tar and residual hydrocracking-delayed coking combination treatment method, comprises following content:
Coal tar, after underpressure distillation, obtains lightweight coal tar and heavy coal tar;
Lightweight coal tar in step (1) and residual oil enter ebullated bed reactor after mixing together with hydrogen, contact with hydrocracking catalyst, carry out hydrocracking reaction;
Step (2) gained hydrocracking effluent enters separator, separates and obtains gas and liquid product, and described liquid product enters separation column fractionation and obtains gasoline, diesel oil, vacuum gas oil and tail oil;
Tail oil in step (3) enters delayed coking unit with together with heavy coal tar in step (1), carries out heat cracking reaction, obtains coking dry gas, coker gasoline, coker gas oil, coker gas oil and coke.
2. it is characterized in that in accordance with the method for claim 1: lightweight coal tar described in step (1) is the cut before underpressure distillation intercepts 480～500 ℃.
3. in accordance with the method for claim 1, it is characterized in that: all or part of ebullated bed reactor that loops back of step (3) gained vacuum gas oil, vacuum gas oil and residual oil circulation weight ratio 0.05～0.18.
4. in accordance with the method for claim 1, it is characterized in that: in step (4), delayed coking gained coker gas oil loops back boiling bed hydrogenation reactor, and coker gas oil and residual oil circulation weight ratio are 0.05～0.25.
5. it is characterized in that in accordance with the method for claim 1: the lightweight coal tar in step (1) enters ebullated bed reactor from the position of one or more different heights of ebullated bed reactor beds along reactor tangential direction.
6. it is characterized in that in accordance with the method for claim 1: in step (2), lightweight coal tar is 1:10～1:1 with the mixed weight ratio of residual oil raw material.
7. in accordance with the method for claim 1, it is characterized in that: in step (2), hydrocracking catalyst is loaded catalyst, wherein, active metal is one or more in nickel, cobalt, molybdenum, tungsten, in metal oxide, nickel or cobalt contents are 1wt%～12wt%, and molybdenum or W content are 2wt%～15wt%.
8. according to the method described in claim 1 or 7, it is characterized in that: in step (2), the character of hydrocracking catalyst is: granules of catalyst diameter is 0.3～0.8mm, and bulk density is 0.6～0.9g/cm
3, specific surface area is 100～280m
2/ g.
9. in accordance with the method for claim 1, it is characterized in that: ebullated bed reactor hydrocracking condition is: 380～450 ℃ of temperature of reaction, reaction pressure 8～20MPa, air speed 0.2～3.0h
-1, hydrogen to oil volume ratio 600～2500.
10. in accordance with the method for claim 9, it is characterized in that: ebullated bed reactor hydrocracking condition is: 400 ℃～440 ℃ of temperature of reaction, reaction pressure 12～16MPa, air speed 0.5～1.5h
-1, hydrogen to oil volume ratio 800～1200.
11. in accordance with the method for claim 1, it is characterized in that: delayed coking unit reaction conditions is: furnace outlet temperature is 450～525 ℃, and coke drum pressure is 0.15～0.35MPa, and recycle ratio is 0.15～0.60.
12. in accordance with the method for claim 1, it is characterized in that: residual oil is one or more in long residuum, vacuum residuum, high viscous crude, visbreaking residue, tar-bitumen, oil sands bitumen, ethylene cracker tar, refinery's sump oil, refinery sludge.
13. in accordance with the method for claim 1, it is characterized in that: coal tar is the viscous liquid product of coal at high temperature carbonization and gasification byproduct in process.
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| CN104087339A (en) * | 2014-06-19 | 2014-10-08 | 北京宝塔三聚能源科技有限公司 | Hydrogenation co-processing method for mixed oil, coal and coal tar |
| CN106753509A (en) * | 2016-11-24 | 2017-05-31 | 辽宁石油化工大学 | A kind of oil sands bitumen blends the visbreaking processing method of dead oil |
| CN108179028A (en) * | 2017-12-25 | 2018-06-19 | 中石化炼化工程（集团）股份有限公司 | A kind of processing of heavy oil method and system |
| CN110408434A (en) * | 2018-04-27 | 2019-11-05 | 中国石油化工股份有限公司 | A kind of method of full fraction of coal tar production needle coke and BTX |
| US11384300B2 (en) | 2019-12-19 | 2022-07-12 | Saudi Arabian Oil Company | Integrated process and system to upgrade crude oil |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4302323A (en) * | 1980-05-12 | 1981-11-24 | Mobil Oil Corporation | Catalytic hydroconversion of residual stocks |
| US6444116B1 (en) * | 2000-10-10 | 2002-09-03 | Intevep, S.A. | Process scheme for sequentially hydrotreating-hydrocracking diesel and vacuum gas oil |
| CN1597866A (en) * | 2004-07-30 | 2005-03-23 | 山西东辉煤焦化集团有限公司 | Process for producing chemical industry products and fuel oil from coal tar |
| CN1880411A (en) * | 2006-03-04 | 2006-12-20 | 荆门市金吉化工有限公司 | Process for preparing fuel oil by using coal tar |
| CN101037618A (en) * | 2007-04-24 | 2007-09-19 | 中国石油化工集团公司 | Coking inhibitor and preparation method and application thereof |
| CN102533332A (en) * | 2012-01-11 | 2012-07-04 | 中国科学院过程工程研究所 | Method for comprehensively using all fractions produced through hydrogenation combined with delayed coking on coal tar |
-
2012
- 2012-10-24 CN CN201210408438.4A patent/CN103773477B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4302323A (en) * | 1980-05-12 | 1981-11-24 | Mobil Oil Corporation | Catalytic hydroconversion of residual stocks |
| US6444116B1 (en) * | 2000-10-10 | 2002-09-03 | Intevep, S.A. | Process scheme for sequentially hydrotreating-hydrocracking diesel and vacuum gas oil |
| CN1597866A (en) * | 2004-07-30 | 2005-03-23 | 山西东辉煤焦化集团有限公司 | Process for producing chemical industry products and fuel oil from coal tar |
| CN1880411A (en) * | 2006-03-04 | 2006-12-20 | 荆门市金吉化工有限公司 | Process for preparing fuel oil by using coal tar |
| CN101037618A (en) * | 2007-04-24 | 2007-09-19 | 中国石油化工集团公司 | Coking inhibitor and preparation method and application thereof |
| CN102533332A (en) * | 2012-01-11 | 2012-07-04 | 中国科学院过程工程研究所 | Method for comprehensively using all fractions produced through hydrogenation combined with delayed coking on coal tar |
Non-Patent Citations (2)
| Title |
|---|
| 李立权: "渣油加氢技术的最新进展及技术路线选择", 《炼油技术与工程》, vol. 40, no. 4, 30 April 2010 (2010-04-30) * |
| 王建明: "渣油深度转化提高轻油收率技术的重大进展", 《中外能源》, vol. 17, no. 8, 31 August 2012 (2012-08-31) * |
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| CN104087339A (en) * | 2014-06-19 | 2014-10-08 | 北京宝塔三聚能源科技有限公司 | Hydrogenation co-processing method for mixed oil, coal and coal tar |
| CN104087339B (en) * | 2014-06-19 | 2015-11-18 | 北京宝塔三聚能源科技有限公司 | A kind of method that assorted oil, coal and coal tar hydrogenating refine altogether |
| CN106753509A (en) * | 2016-11-24 | 2017-05-31 | 辽宁石油化工大学 | A kind of oil sands bitumen blends the visbreaking processing method of dead oil |
| CN108179028A (en) * | 2017-12-25 | 2018-06-19 | 中石化炼化工程（集团）股份有限公司 | A kind of processing of heavy oil method and system |
| CN108179028B (en) * | 2017-12-25 | 2020-03-31 | 中石化炼化工程（集团）股份有限公司 | Heavy oil processing method and system |
| CN110408434A (en) * | 2018-04-27 | 2019-11-05 | 中国石油化工股份有限公司 | A kind of method of full fraction of coal tar production needle coke and BTX |
| CN110408434B (en) * | 2018-04-27 | 2021-03-12 | 中国石油化工股份有限公司 | Method for producing needle coke and BTX from coal tar whole fraction |
| US11384300B2 (en) | 2019-12-19 | 2022-07-12 | Saudi Arabian Oil Company | Integrated process and system to upgrade crude oil |
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