CN106281439A - A kind of method of producing light fuel oil by hydrogenating anthracene oil - Google Patents

A kind of method of producing light fuel oil by hydrogenating anthracene oil Download PDF

Info

Publication number
CN106281439A
CN106281439A CN201610738504.2A CN201610738504A CN106281439A CN 106281439 A CN106281439 A CN 106281439A CN 201610738504 A CN201610738504 A CN 201610738504A CN 106281439 A CN106281439 A CN 106281439A
Authority
CN
China
Prior art keywords
catalyst
carbolineum
oil
hydrocracking
hydrogen
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.)
Pending
Application number
CN201610738504.2A
Other languages
Chinese (zh)
Inventor
杜汉双
齐书奎
张美荣
刘大鹏
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shandong Hengxin Technology Development Co Ltd
Original Assignee
Shandong Hengxin Technology Development Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shandong Hengxin Technology Development Co Ltd filed Critical Shandong Hengxin Technology Development Co Ltd
Priority to CN201610738504.2A priority Critical patent/CN106281439A/en
Publication of CN106281439A publication Critical patent/CN106281439A/en
Pending legal-status Critical Current

Links

Classifications

    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/883—Molybdenum and nickel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/888—Tungsten
    • B01J23/8885—Tungsten containing also molybdenum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/307—Cetane number, cetane index
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure

Abstract

The invention belongs to coalification industrial technical field, a kind of method particularly relating to producing light fuel oil by hydrogenating anthracene oil.A kind of method of producing light fuel oil by hydrogenating anthracene oil, use following steps: raw material carbolineum respectively from A, B two pipeline enter hydrofinishing system, contact with Hydrobon catalyst and carry out hydrofining reaction；The generation oil of hydrofinishing gained carries out gas-liquid separation through high-pressure separator；Liquid product enters hydrocracking reaction district, sequentially passes through after Hydrobon catalyst contacts with hydrocracking catalyst and react, obtains isocrackate；Isocrackate is separated, obtains gasoline and diesel oil distillate.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

A kind of method of producing light fuel oil by hydrogenating anthracene oil
Technical field
The invention belongs to coalification industrial technical field, a kind of method particularly relating to producing light fuel oil by hydrogenating anthracene oil.
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.Chinese invention patent CN101033409A uses two-stage hydrogenation technique, carbolineum After hydrofinishing, by refined products fractional distillation, obtain more than 200 DEG C of fractions as hydrocracking raw material.But said method is with anthracene Oil is raw material, can release substantial amounts of heat in unifining process, there is device temperature rise big, operates jiggly problem, and Easily cause catalyst coking, affect the service life of catalyst.And, gained is refined generates nitrogen content ＜ 400 μ g/g in oil, This just requires the hydrocracking catalyst selecting resistance to nitrogen ability strong, and not only the requirement to hydrocracking catalyst is high, but also limits Make the application of carbolineum hydrocracking process.
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 method of producing light fuel oil by hydrogenating anthracene oil, employing following steps:
(1) raw material carbolineum respectively from A, B two pipeline enter hydrofinishing system, contact with Hydrobon catalyst that to carry out hydrogenation smart System reaction；Enter reactor, carbolineum and hydrogen in B pipeline with hydrogen from finishing reactor top after wherein carbolineum mixes in A pipeline In the middle part of finishing reactor, hydrofinishing system is entered after gas mixing；
In described A pipeline, hydrogen is 1900-2100:1 with the volume ratio of carbolineum, and the flow of carbolineum is 8-9m3/h；Described B manages In road, hydrogen is 1800-1850:1 with the volume ratio of carbolineum, and the flow of carbolineum is 4-5m3/h；
In described finishing reactor, operating condition is: reaction temperature is 260-280 DEG C, volume when pressure is 18.3-19MPa and liquid Air speed is 0.3～0.6h-1；
(2) the generation oil of step (1) hydrofinishing gained carries out gas-liquid separation through high-pressure separator；
(3) liquid product of step (2) gained enters hydrocracking reaction district, in presence of hydrogen, sequentially passes through hydrofinishing Catalyst contacts with hydrocracking catalyst after reacting, and obtains isocrackate；
(4) isocrackate of step (3) gained is separated, obtains gasoline and diesel oil distillate.
Preferably, in the hydrocracking reaction district described in step (3), Hydrobon catalyst and hydrocracking catalyst Admission space accounts for the 30%～60% and 40%～70% of hydrocracking reaction district catalyst total fill able volume respectively.
In described hydrocracking catalyst reaction zone, urge in the filling post processing hydrofinishing of hydrocracking catalyst downstream Agent, its admission space accounts for the 2-5% of hydrocracking reaction district catalyst total fill able volume.Preferably, described post processing adds Hydrogen catalyst for refining component is: tungsten oxide 8-10%, molybdenum oxide 10-15wt%, nickel oxide 7-9wt%, and carrier is aluminium oxide；Its Described in catalyst pore volume be 0.45-0.65ml/g, specific surface area is 130-135m2/g。
Preferably, the carbolineum described in step (1) is the product that high temperature coal-tar obtains through distillation, and its character is as follows: 20 DEG C Density is more than 1.0g/m3, aromatic hydrocarbons and colloid total amount are more than 90wt%, and nitrogen content is more than 1.0wt%, and oxygen content is for being more than 0.9wt%.
Preferably, step (1) or the Hydrobon catalyst component described in step (3) are: molybdenum oxide 18-20wt%, oxygen Changing nickel 7-9wt%, carrier is aluminium oxide；Wherein said catalyst pore volume is 0.40-0.60ml/g, specific surface area 138-145m2/ g。
Preferably, the hydrocracking catalyst described in step (4) is 3936 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 1900-2100: 1.
Beneficial effect
1, the present invention adds carbolineum and hydrogen from the top A pipeline of hydrofining reactor and middle part B pipeline respectively, by controlling Carbolineum and hydrogen ratio and the flow of carbolineum in two pipelines, it is to avoid temperature raises and too fast causes the reaction acutely, compares more straight Connecing and add carbolineum and hydrogen from a pipeline, device temperature rise substantially reduces, and this avoid due to temperature rise, and must be provided with multiple stage Reactor or more beds.
2, the present invention is directed to the feature of carbolineum, select suitable Hydrocracking unit catalyst matching way: be hydrocracked anti- Answer and district loads Hydrobon catalyst and hydrocracking catalyst, so on the one hand can reduce hydrofinishing further and generate oil In colloid, asphalitine and carbon residue, reduce nitrogen and arene content simultaneously, protection hydrocracking catalyst activity, to growing apparatus Service cycle is favourable；On the other hand, more heavier component can be made to be converted into hydrocarbonaceous fuel oil ingredient, improve light-weight fuel oil and receive Rate.
3, in hydrocracking reaction district of the present invention, after hydrocracking catalyst, post processing catalyst for refining, this side are added On the one hand method can reduce the mercaptan generated in product, the very small amount alkene that on the other hand can make generation and the aromatic hydrocarbons reacted the most completely Saturated, to improving, diesel oil distillate Cetane number is favourable.
4, the inventive method is by using suitable technological process and catalyst matching way, can be to greatest extent by anthracene Oil raw material is converted into clean fuel oil component.
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.Raw material carbolineum and hydrogen respectively from A, B two pipeline enter hydrogenation Refining system 1, contacts with Hydrobon catalyst and carries out hydrofining reaction；After wherein in A pipeline, carbolineum mixes with hydrogen from Finishing reactor top enters reactor, enters hydrofinishing with hydrogen after carbolineum mixes in B pipeline in the middle part of finishing reactor System；Reaction effluent 3 enters piece-rate system, after generally comprising high-pressure separator and low pressure separator 4, stripper 5 separation, point The liquid product 6 gone out enters hydrocracking reactor 2, and isocrackate 7 is separated, generally comprises through high-pressure separator and low Pressure separator 8 and stripper 9, isolates liquid product 10 and is fractionated into tower 11 and obtains gasoline fraction 12 and diesel oil distillate 13.Wherein The hydrogen-rich gas that Unit two are separating obtained, after separatory and circulating hydrogen compressor supercharging, a part is mixed with new hydrogen as recycle hydrogen Closing dereaction system, as reaction hydrogen, a part is used for controlling hydrofinishing and hydrocracking reactor catalysis as cold hydrogen Agent bed temperature rise.
Detailed description of the invention
Embodiment 1-3 concrete operations flow process is shown in Fig. 1；Carbolineum character used by embodiment and comparative example is shown in Table 1.
Table 1 raw oil character
Hydrobon catalyst A1:
Component is: molybdenum oxide 18wt%, nickel oxide 9wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume is 0.40ml/ G, specific surface area 145m2/g。
Hydrobon catalyst A2:
Component is: molybdenum oxide 20wt%, nickel oxide 7wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume is 0.60ml/ G, specific surface area 130m2/g。
Hydrobon catalyst A3:
Component is: molybdenum oxide 19wt%, nickel oxide 8wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume is 0.50ml/ G, specific surface area 135m2/g。
Post processing Hydrobon catalyst B1:
Component is: tungsten oxide 8%, molybdenum oxide 15wt%, nickel oxide 7wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume For 0.65ml/g, specific surface area is 138m2/g。
Post processing Hydrobon catalyst B2:
Component is: tungsten oxide 10%, molybdenum oxide 10wt%, nickel oxide 9wt%, and carrier is aluminium oxide；Wherein said catalyst pores Holding is 0.45ml/g, and specific surface area is 140m2/g。
Post processing Hydrobon catalyst B3:
Component is: tungsten oxide 9%, molybdenum oxide 12wt%, nickel oxide 8wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume For 0.55ml/g, specific surface area is 138m2/g。
Comparative example 1
This comparative example carbolineum and hydrogen unlike above-described embodiment 3 only enter from the middle part of hydrofining reactor, other Operating condition is same as in Example 3.
Table 2 embodiment and comparative example technological parameter
Table 3 embodiment and comparative example hydrogenation reaction product slates
Table 4 embodiment and comparative example hydrogenated products character
By table 3 and table 4 it is recognised that by adjusting hydrofinishing system top and middle part carbolineum and the additional proportion of hydrogen and stream Amount, embodiment 1-3 and comparative example product liquid are received (liquid is received as liquefied gas, Petroleum and fuel oil yield summation) and are respectively 94.7%, 93.6%, 96.6% and 79.7%, and tail oil amount is respectively 2.1%, 3.7%, 1.6% and 19.7%.Meanwhile, sulfur with The product index excellence orders such as the content of nitrogen and Cetane number are superior to comparative example for embodiment.

Claims (10)

1. the method for a producing light fuel oil by hydrogenating anthracene oil, it is characterised in that employing following steps:
(1) raw material carbolineum respectively from A, B two pipeline enter hydrofinishing system, contact with Hydrobon catalyst that to carry out hydrogenation smart System reaction；Enter reactor, carbolineum and hydrogen in B pipeline with hydrogen from finishing reactor top after wherein carbolineum mixes in A pipeline In the middle part of finishing reactor, hydrofinishing system is entered after gas mixing；
(2) the generation oil of step (1) hydrofinishing gained carries out gas-liquid separation through high-pressure separator；
(3) liquid product of step (2) gained enters hydrocracking reaction district, in presence of hydrogen, sequentially passes through hydrofinishing Catalyst contacts with hydrocracking catalyst after reacting, and obtains isocrackate；
(4) isocrackate of step (3) gained is separated, obtains gasoline and diesel oil distillate.
Method the most according to claim 1, it is characterised in that hydrogen and the volume of carbolineum in the A pipeline described in step (1) Ratio is 1900-2100:1, and the flow of carbolineum is 8-9m3/h；In described B pipeline, hydrogen is 1800-1850 with the volume ratio of carbolineum: 1, the flow of carbolineum is 4-5m3/h。
Method the most according to claim 1, it is characterised in that in step (1) described finishing reactor, operating condition is: anti- Answering temperature to be 260-280 DEG C, pressure is 18.3-19MPa, and during liquid, volume space velocity is 0.3～0.6h-1。
The most in accordance with the method for claim 1, it is characterised in that in the hydrocracking reaction district described in step (3), hydrogenation essence The admission space of catalyst processed and hydrocracking catalyst accounts for the 30% of hydrocracking reaction district catalyst total fill able volume respectively ～60% and 40%～70%.
5. according to the method described in claim 1 or 4, it is characterised in that in described hydrocracking catalyst reaction zone, adding Hydrogen Cracking catalyst downstream filling post processing Hydrobon catalyst, its admission space accounts for the catalyst general assembly of hydrocracking reaction district Fill out the 2-5% of volume.
The most in accordance with the method for claim 1, it is characterised in that the carbolineum described in step (1) is that high temperature coal-tar is through distillation The product obtained, its character is as follows: 20 DEG C of density are more than 1.0g/m3, aromatic hydrocarbons and colloid total amount are more than 90wt%, and nitrogen content is big In 1.0wt%, oxygen content is more than 0.9wt%.
The most in accordance with the method for claim 1, it is characterised in that the Hydrobon catalyst described in step (1) or step (3) Component is: molybdenum oxide 18-20wt%, nickel oxide 7-9wt%, and carrier is aluminium oxide；Wherein said catalyst pore volume is 0.40- 0.60ml/g, specific surface area 138-145m2/g。
The most in accordance with the method for claim 5, it is characterised in that described post processing Hydrobon catalyst component is: oxidation Tungsten 8-10%, molybdenum oxide 10-15wt%, nickel oxide 7-9wt%, carrier is aluminium oxide；Wherein said catalyst pore volume is 0.45- 0.65ml/g, specific surface area is 130-135m2/g。
The most in accordance with the method for claim 1, it is characterised in that the hydrocracking catalyst described in step (4) is 3936 catalysis Agent.
The most in accordance with the method for claim 1, it is characterised in that the hydrocracking operation condition described in step (4), hydrogenation splits Change reaction pressure is 13-14MPa, reaction temperature is 275-280 DEG C, reaction velocity is 0.9-1.0h-1, hydrogen to oil volume ratio be 1900-2100∶1。
CN201610738504.2A 2016-08-29 2016-08-29 A kind of method of producing light fuel oil by hydrogenating anthracene oil Pending CN106281439A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610738504.2A CN106281439A (en) 2016-08-29 2016-08-29 A kind of method of producing light fuel oil by hydrogenating anthracene oil

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610738504.2A CN106281439A (en) 2016-08-29 2016-08-29 A kind of method of producing light fuel oil by hydrogenating anthracene oil

Publications (1)

Publication Number Publication Date
CN106281439A true CN106281439A (en) 2017-01-04

Family

ID=57677110

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610738504.2A Pending CN106281439A (en) 2016-08-29 2016-08-29 A kind of method of producing light fuel oil by hydrogenating anthracene oil

Country Status (1)

Country Link
CN (1) CN106281439A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111234868A (en) * 2020-02-13 2020-06-05 中国科学院青岛生物能源与过程研究所 Method for producing high-energy hydrocarbon fuel by treating anthracene oil

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6299759B1 (en) * 1998-02-13 2001-10-09 Mobil Oil Corporation Hydroprocessing reactor and process with gas and liquid quench
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

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6299759B1 (en) * 1998-02-13 2001-10-09 Mobil Oil Corporation Hydroprocessing reactor and process with gas and liquid quench
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 (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111234868A (en) * 2020-02-13 2020-06-05 中国科学院青岛生物能源与过程研究所 Method for producing high-energy hydrocarbon fuel by treating anthracene oil
CN111234868B (en) * 2020-02-13 2023-12-22 中国科学院青岛生物能源与过程研究所 Method for producing high-energy hydrocarbon fuel by anthracene oil treatment

Similar Documents

Publication Publication Date Title
CN103265971B (en) Heterogeneous coal tar suspension bed hydrogenation method
CN102796559B (en) Method and the device of oil fuel are produced in hydrocracking
CN102604677B (en) High and low-temperature Fischer-Tropsch synthesis co-production technology
CN104962307B (en) Method for producing light oil through coal liquefaction
CN101781577B (en) Method for producing lightweight fuel oil by utilizing mixed coal tar
CN104194830B (en) Direct coal liquefaction circulating solvent and processing method thereof as well as direct coal liquefaction method utilizing direct coal liquefaction circulating solvent
CN101240191B (en) Method for producing lightweight fuel oil by coal tar heavy fractioning hydrogenation
CN102041075A (en) Anthracene oil hydrogenation method
CN101962572A (en) Coal tar heavy fraction fluidized-bed hydrocracking method and system thereof
CN104277879B (en) A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar
CN106221792A (en) A kind of anthracene oil hydrogenation method
CN110257102A (en) A kind of raw material classification rich in polycyclic aromatic hydrocarbon faces hydrogen pyrolysis and produces the production system and method for light aromatics
CN102041073A (en) Hydrocracking method for anthracene oil
CN103864564B (en) Technique for processing methanol-to-propylene by-products
CN108102709A (en) The processing and treating method of catalytic diesel oil
KR102256614B1 (en) Process and apparatus for separating c5 di-olefins from pyrolysis gasoline
CN109355100B (en) Coal tar processing and coal co-refining combined process
CN106281439A (en) A kind of method of producing light fuel oil by hydrogenating anthracene oil
CN104449836A (en) Trans-hydrocracking process of whole fractions of coal tar
CN103864563B (en) Method for preparing aromatic hydrocarbon from hydrocarbon tail oil byproducts produced in coal-based methanol to propylene process
CN105623731A (en) Method for preparing high-density coal-based jet fuel by adopting anthracene oil as raw material
CN109777495B (en) Refinery gas combined processing method
CN102585898A (en) High-nitrogen high-aromatic-oil two-stage method hydrocarbon hydrogenation method
CN105087047B (en) A kind of heavy oil catalytic cracking process of fecund weight aromatic hydrocarbon product
CN104277878B (en) A kind of two-stage slurry state bed hydroprocessing technique of high temperature coal-tar

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication
RJ01 Rejection of invention patent application after publication

Application publication date: 20170104