CN106221792A - A kind of anthracene oil hydrogenation method - Google Patents
A kind of anthracene oil hydrogenation method Download PDFInfo
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- CN106221792A CN106221792A CN201610738503.8A CN201610738503A CN106221792A CN 106221792 A CN106221792 A CN 106221792A CN 201610738503 A CN201610738503 A CN 201610738503A CN 106221792 A CN106221792 A CN 106221792A
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The invention belongs to coalification industrial technical field, particularly relate to a kind of anthracene oil hydrogenation method.Anthracene oil hydrogenation method uses following steps: after carbolineum hydrofinishing, separates through high pressure hot separator, and liquid product enters thermal low-pressure separators, and low point of oil of heat is partly recirculated to hydrofining reactor；Low point of oil of remainder heat enters hydrocracking reactor, obtain isocrackate, isocrackate enters cold high pressure separator with from the isolated gas of high pressure hot separator, the gas that the liquid that cold high pressure separator separates and thermal low-pressure separators sub-argument go out enters cold low separator and carries out further gas-liquid separation, and the cold low point of oil that cold low separator separates is partly recirculated to hydrofining reactor；Cold low point of oil of remainder, carries out fractional distillation, obtains various product and tail oil.The method refining stage temperature rise is little, smooth operation, and the method not only can make carbolineum hydrogenation produce lightweight vapour, diesel product, and makes device operational security steady, extension fixture service cycle.
Description
Technical field
The invention belongs to coalification industrial technical field, particularly relate to a kind of anthracene oil hydrogenation method.
Background technology
Carbolineum is an important part for coal tar component, and in recent years, coal tar hydrogenating receives much concern in coal chemical industry, with
Each fraction of coal tar is that raw material Hydrogenation has been reported for clean fuel oil.
Carbolineum is one of fraction of high temperature coal-tar distillation gained, its initial boiling point at 220～260 DEG C, the end point of distillation 500～
550 DEG C, boiling range is heavier, belongs to heavy distillat scope.The mixture that carbolineum is mainly made up of compounds such as anthracene, phenanthrene, carbazole, acenaphthenes, greatly
Mostly being the aromatic hydrocarbons at more than three rings and Fourth Ring, density (20 DEG C) is more than 1.0g/m3, and impurity content is high, and especially nitrogen content exists
About 1wt%, the highest, oxygen content is higher, generally 0.9～1.3wt%, and carbolineum is a kind of spy being different from petroleum distillate
Different raw material.
The purposes of carbolineum is used as carbon black raw material or for coal-tar creosote solution at present, or isolated anthracene, acenaphthene, phenanthrene, carbazole
Deng product, but the added value of said method is the most relatively low.
In prior art, Chinese patent literature CN102041075A discloses the method for a kind of carbolineum hydrogenation, and the method is
Carbolineum is hydrogenated refined, then carries out gas-liquid separation through high pressure hot separator and thermal low-pressure separators, low point of oily part of the heat of gained
Loop back hydrofining reaction district to mix with carbolineum, remainder hot Di Fenyouqu hydrocracking reaction district, isocrackate
Entering cold high pressure separator with from the isolated gas of high pressure hot separator, the liquid separated is isolated with thermal low-pressure separators
Gas enters cold low separator, and the liquid separated removes product fractionating column after stripping, obtains gasoline and fuel oil.During,
The hydrogen-rich gas that cold high pressure separator separates, after separatory and compressor boost, uses as recycle hydrogen, and recycle hydrogen mixes with new hydrogen
Can be as carbolineum hydrofinishing unit and Hydrocracking unit reactor inlet hydrogen after conjunction, it is also possible to be used for controlling as cold hydrogen
Hydrofinishing processed and hydrocracking reactor beds temperature rise.Said method, utilizes recycle hydrogen cooling to reduce hydrogenation essence
Intensification during system, extends the life-span of Hydrobon catalyst, improves the quality of carbolineum hydrogenation products, but or needs
To reapply after recycle hydrogen and new hydrogen are mixed in hydrofinishing section, to increase hydrogen in hydrofinishing section by the new hydrogen of addition and divide
Pressure, the new hydrogen of addition needs could use after hydrogen purification device purifies, adds the complexity of hydrogenation system, improves
Cost.
Summary of the invention
For overcoming the deficiencies in the prior art, the invention provides a kind of anthracene oil hydrogenation method, the method refining stage temperature rise is little,
Smooth operation, the method not only can make carbolineum hydrogenation produce lightweight vapour, diesel product, and make device operational security steady, prolong
Growth device service cycle.
A kind of anthracene oil hydrogenation method, employing following steps:
(1) in presence of hydrogen, carbolineum enters hydrofining reactor, contacts with Hydrobon catalyst that to carry out hydrofinishing anti-
Should；
(2) the generation oil of step (1) hydrofinishing gained carries out gas-liquid separation through high pressure hot separator；
(3) liquid product that step (2) high pressure hot separator separates enters thermal low-pressure separators and carries out further gas-liquid separation, heat
Low point of oil of the heat that low pressure separator separates is partly recirculated to hydrofining reactor；
(4) low point of oil of step (3) remainder heat enters hydrocracking reactor, in presence of hydrogen, hydrogenated cracking catalysis
After agent reaction, obtain isocrackate；
(5) isocrackate of step (4) gained separates with from high pressure hot separator isolated gas entrance cold anticyclone
Device；
(6) step (5) cold high pressure separator carries out gas-liquid separation, and the liquid separated gas isolated with thermal low-pressure separators enters
Entering cold low separator and carry out further gas-liquid separation, the cold low point of oil that cold low separator separates is partly recirculated to hydrofinishing
Reactor；
(7) by cold low point of oil of step (6) remainder, carry out fractional distillation, obtain various product and tail oil.
Cold low point of oil circulation time hydrofining reactor described in low point of oil of heat described in step (3) and step (6) total
Weight is 2-3:1 with the weight ratio of carbolineum；Low point of oil of heat and step (6) that wherein step (3) is recycled in hydrogenation reactor are followed
Ring is 1:1.5-2.5 to cold low point of oily mass ratio in hydrogenation reactor.
The hydrogen-rich gas that above-mentioned cold high pressure separator separates, after separatory and compressor boost, uses as recycle hydrogen, or
Person is as cold hydrogen.
Described hydrofinishing operating condition, to fresh feed: reaction temperature 405～410 DEG C, pressure 18～19MPa, hydrogen
Oil volume is than 1200: 1～1600: 1 and air speed 0.3～0.6h-1。
Preferably, beds is set, in described hydrofining reactor between catalyst bed top and bed all
Cold hydrogen inlet, beds filling hydrogenation catalyst, consisting of in described hydrogenation catalyst: molybdenum oxide 18-are set
20wt%, nickel oxide 7-9wt%, carrier is aluminium oxide；Wherein said catalyst pore volume is 0.40-0.60ml/g, specific surface area
For 130-145m2/ g, catalyst amount is 85-95 μ g/g.
Beds, catalyst bed top and each catalyst are set in the hydrocracking reactor described in step (4)
It is respectively provided with cold hydrogen inlet between bed, and loads Cracking catalyst；Wherein said Cracking catalyst is 3976 catalyst.
Hydrocracking operation condition described in step (4), hydrocracking reaction total system pressure is 13-14MPa, reaction temperature
Degree is 275-280 DEG C, reaction velocity is 0.9-1.0h-1, hydrogen to oil volume ratio be 1900: 1-2100: 1.
Beneficial effect
1, the present invention uses part low point of oil of heat and cold low point of oil circulation time hydrofining reactor, with carbolineum together as hydrogenation
The charging in refining reaction district, so, on the one hand effectively reduces the arene content in hydrofining reactor charging, makes device temperature
Rise and substantially reduce, can avoid due to temperature rise, and must be provided with multiple stage reactor or more beds；On the other hand, add
The hydrogen consumed in hydrogen course of reaction, is filled into by the section of being hydrocracked, can improve hydrogen purity in the section of being hydrocracked hydrogen gas circulating system,
Improve the hydrogen dividing potential drop of Hydrocracking unit；In combination with accurate hydrofinishing and hydrocracking reaction condition (hydrogen-oil ratio,
Reaction temperature etc.), improve reaction depth and hydrogenation effect.
2, the inventive method Optimizing Flow, compared with conventional two-stage reforming technique, only need to be with a recycle hydrogen compression
Machine just can obtain returning the recycle hydrogen of two reaction zones, reduces the most again by a circulating hydrogen compressor.This two aspect all can be the biggest
Equipment investment is saved in degree.
3, the present invention uses low point of oil of heat and cold low point of oil circulation time hydrofinishing unit, can effectively reduce in carbolineum raw material
Colloid and the concentration of carbon residue, play favorably hydrofinishing and the permanent of hydrocracking catalyst activity, can realize the length of device
Cycle keeps the safety in production.
4, the present invention uses low point of oil of heat and cold low point of oil circulation time hydrofinishing unit, utilizes the similar principle that mixes, makes
The concentration of high melting compound anthracene, phenanthrene, carbazole and pyrene in carbolineum reduces, and reduces and feed system is incubated uniformity requirement
Severe, make device smooth and easy charging under being similar to paraffin device holding temperature.
Accompanying drawing explanation
Fig. 1 is the schematic flow diagram of anthracene oil hydrogenation method of the present invention.
In conjunction with Fig. 1, the inventive method is described further.After the hydrogenated finishing reactor of carbolineum 1, gained hydrofinishing
Generating oil and carry out gas-liquid separation through high pressure hot separator 2, the liquid product separated enters thermal low-pressure separators 3 and carries out further gas
Liquid separates, and low point of oil 11 part of heat loops back hydrofining reactor, and remainder low point of oil 11 of heat directly goes to be hydrocracked instead
Answering district to make raw material, after hydrogenated catalyst for refining, obtain isocrackate 16, isocrackate 16 separates with from thermal high
The isolated hot high score gas 14 of device 2 mixes, and enters cold high pressure separator 4.Come from the hydrogen-rich gas 13 of cold high pressure separator
Through circulating hydrogen compressor 12 supercharging, as recycle hydrogen 13 dereaction system, as carbolineum hydrofinishing unit be hydrocracked list
Elementary reaction device entrance hydrogen, it is also possible to be used for controlling hydrofinishing and hydrocracking reactor beds temperature as cold hydrogen
Rise.Low point of gas 17 of the isolated liquid of cold high pressure separator 4 heat isolated with thermal low-pressure separators enters cold low and separates
Device 5.The isolated liquid portion of cold low separator 5 loops back hydrofining reactor, the cold low point of oil product warp of remainder
Product stripper 7 stripping removing hydrogen sulfide and gas products 18, stripping tower bottom liquid removes product fractionating column 8, produces vapour through distillation
Oil distillate 9 and diesel oil distillate 19.
Detailed description of the invention
Embodiment 1-3 all uses two-stage reforming technique, concrete operations flow process to see Fig. 1；Used by embodiment and comparative example
Carbolineum character is shown in Table 1.
Embodiment 1
The present embodiment loops back the weight of low point of oil of heat of hydrofining reactor and cold low point of oily gross weight and raw material carbolineum
Amount ratio is 2:1；The hottest low point of oil and cold low point of oily mass ratio are 1:1.5.
The condition of hydrofining reaction is: reaction temperature is 405 DEG C, pressure is 18MPa, hydrogen to oil volume ratio is 1200: 1 Hes
Air speed is 0.3h-1, the composition of Hydrobon catalyst and character is: molybdenum oxide 18wt%, nickel oxide 9wt%, and carrier is oxidation
Aluminum；Wherein said catalyst pore volume is 0.40ml/g, and specific surface area is 130m2/ g, catalyst amount is 85 μ g/g (every gram of hydrogenation
Tenor in the catalyst that raw material needs).
Hydrocracking reaction total system pressure is 14MPa, reaction temperature is 280 DEG C, reaction velocity is 1.0h-1, standard body
Long-pending hydrogen-oil ratio 2100:1, Cracking catalyst is 3976 catalyst.
Embodiment 2
The present embodiment loops back the weight of low point of oil of heat of hydrofining reactor and cold low point of oily gross weight and raw material carbolineum
Amount ratio is 3:1；The hottest low point of oil and cold low point of oily mass ratio are 1:1.5.
The condition of hydrofining reaction is: reaction temperature 410 DEG C, pressure 19MPa, hydrogen to oil volume ratio 1600: 1 and air speed
0.6h-1, the composition of Hydrobon catalyst and character is: molybdenum oxide 20wt%, nickel oxide 7wt%, carrier is aluminium oxide；Wherein
Described catalyst pore volume is 0.60ml/g, and specific surface area is 145m2/ g, catalyst amount is that (every gram of hydrogenating materials needs 95 μ g/g
Tenor in the catalyst wanted).
Hydrocracking operation condition, hydrocracking reaction total system pressure is 13MPa, reaction temperature is 275 DEG C, reaction sky
Speed is 0.9h-1, hydrogen to oil volume ratio be 1900: 1, Cracking catalyst is 3976 catalyst.
Embodiment 3
The present embodiment loops back the weight of low point of oil of heat of hydrofining reactor and cold low point of oily gross weight and raw material carbolineum
Amount ratio is 3:1；The hottest low point of oil and cold low point of oily mass ratio are 1:2.
The condition of hydrofining reaction is: reaction temperature 405 DEG C, pressure 19MPa, hydrogen to oil volume ratio 1500: 1 and air speed
0.5h-1, the composition of Hydrobon catalyst and character is: molybdenum oxide 19wt%, nickel oxide 8wt%, carrier is aluminium oxide；Wherein
Described catalyst pore volume is 0.50ml/g, and specific surface area is 138m2/ g, catalyst amount is that (every gram of hydrogenating materials needs 90 μ g/g
Tenor in the catalyst wanted).
Hydrocracking operation condition, hydrocracking reaction total system pressure is 13MPa, reaction temperature is 280 DEG C, reaction sky
Speed is 0.9h-1, hydrogen to oil volume ratio be 1900: 1-2000: 1, Cracking catalyst is 3976 catalyst.
Comparative example 1
What this comparative example was unlike the embodiments above is that the isolated liquid of cold low separator is not recycled to hydrofining reaction
Device, fully enters product gas tower and processes.Other operating conditions are same as in Example 3.
Table 1 raw oil character
Table 2 embodiment and comparative example hydrogenation reaction product slates
Table 3 embodiment and comparative example hydrogenated products character
Test raw material anthracene oil properties used by embodiment 1-3 and comparative example is as shown in table 1.By adjusting hydrofinishing and hydrogenation
Cracking hydrogen gas circulating system and new hydrogen fill into difference, embodiment 1-3 and comparative example product liquid receipts, and (liquid is received as liquefied gas, Petroleum
With fuel oil yield summation) it is respectively 95 .6%, 94.5%, 96.1% and 81.6%, and tail oil amount is respectively 1.9%,
3.3%, 1.1% and 17.9%.Meanwhile, the product index excellence order such as the content of sulfur and nitrogen and Cetane number is that embodiment is the most excellent
In comparative example.
In sum, the anthracene oil hydrogenation method of the present patent application, under meeting refining stage hydrogen purity and hydrogen dividing potential drop, low point of heat
Oily and cold low point of oil circulation time hydrogenation stands device, fills into the hydrogen gas circulating system of cracking and new hydrogen by adjusting to refine, heightens
The hydrogen purity of cracking zone and hydrogen dividing potential drop, can increase reaction depth, improves product liquid and receives and quality, reduces tail oil amount.
Claims (7)
1. an anthracene oil hydrogenation method, it is characterised in that employing following steps:
(1) in presence of hydrogen, carbolineum enters hydrofining reactor, contacts with Hydrobon catalyst that to carry out hydrofinishing anti-
Should；
(2) the generation oil of step (1) hydrofinishing gained carries out gas-liquid separation through high pressure hot separator；
(3) liquid product that step (2) high pressure hot separator separates enters thermal low-pressure separators and carries out further gas-liquid separation, heat
Low point of oil of the heat that low pressure separator separates is partly recirculated to hydrofining reactor；
(4) low point of oil of step (3) remainder heat enters hydrocracking reactor, in presence of hydrogen, hydrogenated cracking catalysis
After agent reaction, obtain isocrackate；
(5) isocrackate of step (4) gained enters cold high pressure separator with from the isolated gas of high pressure hot separator；
(6) step (5) cold high pressure separator carries out gas-liquid separation, and the liquid separated gas isolated with thermal low-pressure separators enters
Entering cold low separator and carry out further gas-liquid separation, the cold low point of oil that cold low separator separates is partly recirculated to hydrofinishing
Reactor；
(7) by cold low point of oil of step (6) remainder, carry out fractional distillation, obtain various product and tail oil.
A kind of anthracene oil hydrogenation method the most according to claim 1, it is characterised in that low point of oil of the heat described in step (3) and
The gross mass of cold low point of oil circulation time hydrofining reactor described in step (6) and the mass ratio of raw material carbolineum are 2-3:1；Its
Low point of oil of the heat that middle step (3) is recycled in hydrogenation reactor and step (6) be recycled in hydrogenation reactor cold low point is oily
Mass ratio is 1:1.5-2.5.
A kind of anthracene oil hydrogenation method the most according to claim 1, it is characterised in that the cold anticyclone described in step (6) separates
The hydrogen-rich gas that device separates, after separatory and compressor boost, uses as recycle hydrogen, or as cold hydrogen.
Method the most according to claim 1, it is characterised in that the hydrofinishing operating condition described in step (1), to fresh
Charging: reaction temperature 405～410 DEG C, pressure 18～19MPa, hydrogen to oil volume ratio 1200: 1～1600: 1 and air speed 0.3～
0.6h-1。
Method the most according to claim 1, it is characterised in that in the hydrofining reactor described in step (1), catalysis is set
Agent bed, is respectively provided with cold hydrogen inlet between catalyst bed top and bed, beds filling hydrogenation catalyst, described in add
Consisting of in hydrogen catalyst: molybdenum oxide 18-20wt%, nickel oxide 7-9wt%, carrier is aluminium oxide；Wherein said catalyst
Pore volume is 0.40-0.60ml/g, and specific surface area is 130-145m2/ g, catalyst amount is 85-95 μ g/g.
Method the most according to claim 1, it is characterised in that in the hydrocracking reactor described in step (4), catalysis is set
Agent bed, is respectively provided with cold hydrogen inlet, and loads Cracking catalyst between catalyst bed top and each beds；Wherein
Described Cracking catalyst is 3976 catalyst.
Method the most according to claim 1, it is characterised in that the hydrocracking operation condition described in step (4), hydrogenation splits
Change response system gross pressure be 13-14MPa, reaction temperature be 275-280 DEG C, reaction velocity be 0.9-1.0h-1, hydrogen to oil volume ratio
It is 1900: 1-2100: 1.
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| CN201610738503.8A CN106221792A (en) | 2016-08-29 | 2016-08-29 | A kind of anthracene oil hydrogenation method |
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| CN201610738503.8A CN106221792A (en) | 2016-08-29 | 2016-08-29 | A kind of anthracene oil hydrogenation method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240934A (en) * | 2019-06-26 | 2019-09-17 | 北京石油化工工程有限公司 | Two-stage hydrogenation reaction system and method |
| CN113801691A (en) * | 2020-06-12 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for producing ethylene device raw material from residual oil |
| WO2022011868A1 (en) * | 2020-07-16 | 2022-01-20 | 南京延长反应技术研究院有限公司 | Reaction system and method for hydrogenation of anthracene oil |
| CN115678593A (en) * | 2022-10-31 | 2023-02-03 | 山东恒信科技发展有限公司 | Coal tar hydrocracking process |
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| CN102041075A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Anthracene oil hydrogenation method |
| CN103571533A (en) * | 2012-07-20 | 2014-02-12 | 中国石油化工集团公司 | Coal tar hydrogenation system and coal tar hydrogenation method |
| CN105462610A (en) * | 2015-11-23 | 2016-04-06 | 华电重工股份有限公司 | Anthracene oil hydrogenation method |
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2016
- 2016-08-29 CN CN201610738503.8A patent/CN106221792A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041075A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Anthracene oil hydrogenation method |
| CN103571533A (en) * | 2012-07-20 | 2014-02-12 | 中国石油化工集团公司 | Coal tar hydrogenation system and coal tar hydrogenation method |
| CN105462610A (en) * | 2015-11-23 | 2016-04-06 | 华电重工股份有限公司 | Anthracene oil hydrogenation method |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240934A (en) * | 2019-06-26 | 2019-09-17 | 北京石油化工工程有限公司 | Two-stage hydrogenation reaction system and method |
| CN110240934B (en) * | 2019-06-26 | 2024-03-26 | 北京石油化工工程有限公司 | Two-stage hydrogenation reaction system and method |
| CN113801691A (en) * | 2020-06-12 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for producing ethylene device raw material from residual oil |
| CN113801691B (en) * | 2020-06-12 | 2023-07-28 | 中国石油化工股份有限公司 | Method and system for producing ethylene plant raw material from residual oil |
| WO2022011868A1 (en) * | 2020-07-16 | 2022-01-20 | 南京延长反应技术研究院有限公司 | Reaction system and method for hydrogenation of anthracene oil |
| CN115678593A (en) * | 2022-10-31 | 2023-02-03 | 山东恒信科技发展有限公司 | Coal tar hydrocracking process |
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Application publication date: 20161214 |