CN105462610B - A kind of anthracene oil hydrogenation method - Google Patents
A kind of anthracene oil hydrogenation method Download PDFInfo
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- CN105462610B CN105462610B CN201510818793.2A CN201510818793A CN105462610B CN 105462610 B CN105462610 B CN 105462610B CN 201510818793 A CN201510818793 A CN 201510818793A CN 105462610 B CN105462610 B CN 105462610B
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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
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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Abstract
The invention discloses a kind of anthracene oil hydrogenation method.Methods described mixes with entrance hydrogen after carbolineum is diluted with low point of oil of heat and carries out hydrofining reaction, obtains hydrofinishing product and obtains refined hot low point of oil through separation；The refined hot low point of oil in part is mixed with entrance hydrogen, then hydrocracking reaction is carried out after filling into new hydrogen, the cold high score oil of cracking is obtained after obtaining the separation of hydrocracking reaction product；By the cold high score oil of cracking with carrying out separating to obtain cold low point of oil after refined cold high score oil mixing；Cold low point of oil is carried out being fractionated to obtain product.The method of the present invention introduces entrance hydrogen by hydrofinishing section, the method that new hydrogen is filled into by being hydrocracked section, it have adjusted the addition point of hydrogen gas circulating system and new hydrogen, it ensure that the hydrogen purity and hydrogen dividing potential drop in hydrogen gas circulating system, improve hydrofinishing and be hydrocracked depth, product liquid receipts are improved, reduce tail oil amount, technological process is simple, the operating of high conversion rate, device is stable.
Description
Technical field
The invention belongs to carbolineum hydrogenation technique field, and in particular to a kind of anthracene oil hydrogenation method.
Background technology
Coal tar is the accessory substance that coal is formed in coking, gasification and retort process, contains substantial amounts of alkene, polycyclic aromatic hydrocarbon
Deng unsaturated hydrocarbons and sulphur, nitrogen compound, acidity is high, gum level is high.Carbolineum is high temperature coal-tar through 280 DEG C of distillation cutting~
360 DEG C of cut, mainly it is made up of anthracene, phenanthrene, carbazole, firefly anthracene and pyrene etc. dystectic three, four aromatic compounds.For carbolineum
Reprocessing, it is mainly former by concentration, solvent extraction or distillation extraction crude anthracene, phenanthrene, the industrial chemicals such as carbazole, or configuration carbon black
Material oil, road asphalt and fuel oil etc..
At present, domestic fuel oil market increasingly increases the demand of fuel oil, and price rises steadily, and petroleum resources
But relative shortage.Therefore, it is that one kind has coking by-productses carbolineum to be carried out into hydrotreating production naphtha and diesel oil blending component
Effect improves the approach of carbolineum added value.By using hydrogenation technique, it can effectively realize that desulfurization, unsaturated hydrocarbons saturation, denitrogenation are anti-
Answer, aromatic hydrocarbons saturation, so as to improving the stability of carbolineum, reducing sulphur nitrogen content and reducing arene content, obtain the stone of high-quality
Cerebrol and diesel oil blending component.
In the prior art, the technique of carbolineum hydrogenation mainly has hydrofinishing, is hydrocracked or both two sections of combination plus
Hydrogen technique.In two-stage hydrogenation technique, selection of the hydrofinishing for catalyst using the Ni-Mo series catalysts of high desulfurization activity as
Main, the stabilization of catalyst directly affects the effect of hydrofinishing, but the big calorimetric discharged in unifining process can cause
Device heating is larger, operation is unstable and causes catalyst coking, influences the service life of catalyst.Through first paragraph process for refining
After processing, nitrogen content in the refined generation oil of gained<400 μ g/g, so high nitrogen content can be in second segment process to urging
Agent stability impacts, so this requires the hydrocracking catalyst for selecting resistance to nitrogen ability strong in hydrocracking process
Agent, so as to further reduce the range of choice of hydrocracking catalyst and the application of hydrocracking process.
In the prior art, Chinese patent literature CN102041075A discloses a kind of method of carbolineum hydrogenation, and this method is
Carbolineum is hydrogenated refined, then carries out gas-liquid separation, the hot low point of oily part of gained through high pressure hot separator and thermal low-pressure separators
It is recycled back to hydrofining reaction area to mix with carbolineum, the hot Di Fenyouqu hydrocracking reactions area of remainder, isocrackate
Enter cold high pressure separator with the gas isolated from high pressure hot separator, what the liquid separated was 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 uses after liquid separation and compressor boost as recycle hydrogen, and recycle hydrogen mixes with new hydrogen
Carbolineum hydrofinishing unit and Hydrocracking unit reactor inlet hydrogen can be used as after conjunction, cold hydrogen can also be used as to be used to control
Hydrofinishing processed and hydrocracking reactor beds temperature rise.The above method, hydrogenation essence is reduced using recycle hydrogen cooling
Heating during system, the life-span of Hydrobon catalyst is extended, improve the quality of carbolineum hydrogenation products, but still needed
Reapplied after recycle hydrogen and new hydrogen are mixed in hydrofinishing section, increase hydrogen point by adding new hydrogen in hydrofinishing section
Pressure, the new hydrogen of addition need to use after hydrogen purification device is purified, and add the complexity of hydrogenation system, improve
Cost.
The content of the invention
Therefore, the technical problem to be solved in the present invention is during overcoming two-stage hydrogenation of the prior art that recycle hydrogen divides
Press relatively low, hydrogenation reaction is not thorough, and hydrogenation liquid receives the defects of relatively low, and so as to provide, a kind of technological process and equipment be simple, conversion
A kind of high anthracene oil hydrogenation method of rate.
Therefore, technical scheme is as follows：
A kind of anthracene oil hydrogenation method, comprises the following steps：
(1) by the low point of oil dilution of carbolineum heat；
(2) carbolineum after step (1) is diluted is mixed with entrance hydrogen, and hydrogenation essence is carried out under Hydrobon catalyst effect
System reaction, obtains hydrofinishing product；
(3) the hydrofinishing product obtained by step (2) is obtained through separation refine cold gas separated by high pressure separator, refined cold high score oil,
Refined low point of gas of heat and refined hot low point of oil；
(4) the refined hot low point of oil in part is mixed with entrance hydrogen, then after filling into new hydrogen, in the case where hydrocracking catalyst acts on
Hydrocracking reaction is carried out, obtains hydrocracking reaction product；
(5) separation is carried out to hydrocracking reaction product and obtains the cold gas separated by high pressure separator of cracking and the cold high score oil of cracking；By cracking
Cold high score oil after the refined cold high score oil mixing in step (3) with carrying out separating to obtain cold low point of gas and cold low point of oil；
(6) by the cold low point of oil obtained by step (5), it is fractionated, obtains various products and tail oil；
In above-mentioned anthracene oil hydrogenation method, the pressure of the entrance hydrogen is 18.3MPa, includes the group of following molar percentage
Point：H2S 1.00-1.13%, NH30.85-0.91%, H294.20-94.39% and CH42.50-2.68%.
In above-mentioned anthracene oil hydrogenation method, the cold gas separated by high pressure separator of cracking is mixed with cold refined gas separated by high pressure separator and delivers to circulating hydrogen compressor liter
18.3MPa is depressed into as recycle hydrogen；The recycle hydrogen as the cold hydrogen of finishing reactor and cracker beds, plus
The refined entrance hydrogen with hydrocracking reaction of hydrogen；
In above-mentioned anthracene oil hydrogenation method, the condition of hydrofinishing is in step (2)：Reaction gross pressure is 18MPa, standard body
Product hydrogen-oil ratio is 800~1500m3/m3(oil volume 1, similarly hereinafter), reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.1
~5.0h-1。
In above-mentioned anthracene oil hydrogenation method, beds, beds top are set in the hydrofining reactor
Cold hydrogen inlet, beds filling hydrogenation catalyst, the active component of the hydrogenation catalyst are respectively provided between bed
For VI B and the metallic compound or its aqueous solution of group VIII one or more, carrier is silica or aluminum oxide；It is described to urge
Agent pore volume is 0.20~0.50ml/g, 100~200m of specific surface area2/ g, catalyst charge are calculated as 50~200 μ with metal
G/g (tenor in the catalyst that every gram of hydrogenating materials need).
Preferably, the catalyst charge is calculated as 60~150 μ g/g with metal, optimal for 80~100 μ g/g.
In above-mentioned anthracene oil hydrogenation method, the active component content of the catalyst is：Vib metals content is with metal oxygen
Compound is calculated as 5wt%~25wt%, and group VIII tenor is calculated as 1wt%~10wt% with metal oxide.
In above-mentioned anthracene oil hydrogenation method, the process of the separation of hydrofinishing product described in step (2) includes：Will hydrogenation essence
Product processed enters high pressure hot separator, is separated into hot high score vapour and hot high score oil；Hot high score vapour enters cold high pressure separator, point
It is oily to refine cold gas separated by high pressure separator and refined cold high score；Hot high score oil enters thermal low-pressure separators, be separated into refined low point of gas of heat with
Low point of oil of refined heat.
In above-mentioned anthracene oil hydrogenation method, the hydrocracking reactor described in step (4) is anti-for air-liquid parallel type fixed bed
Answer device；Reaction condition is：Reaction temperature is 260~340 DEG C, and reaction gross pressure is 18MPa, and reaction velocity is 0.1~4.0h-1,
Normal volume hydrogen-oil ratio is 1000~3000m3/m3。
In above-mentioned anthracene oil hydrogenation method, it is respectively provided between the hydrocracking reactor top and each beds cold
Hydrogen inlet, and load Cracking catalyst；In Cracking catalyst, active material for cobalt, molybdenum or nickel oxide in one kind or
Several, carrier is aluminum oxide, sieve and silica-sesquioxide or molecular sieve.
In above-mentioned anthracene oil hydrogenation method, the refined hot low point of oil in the part is recycled to hydrofinishing section and diluted as carbolineum
Oil；The tail oil is recycled to hydrofinishing section as carbolineum flux oil.
Technical solution of the present invention, have the following advantages that：
1. anthracene oil hydrogenation method provided by the invention, using carbolineum distillate as raw material, by hydrofinishing, it is hydrocracked
It is in parallel to circulate hydrogen system, new hydrogen is filled into by being hydrocracked section, the method that hydrofinishing section introduces entrance hydrogen, have adjusted hydrogen circulation
The addition point of system and new hydrogen, hydrogen purity and hydrogen dividing potential drop in hydrogen gas circulating system are ensure that, improve hydrofinishing and add
Hydrogen cracking level, product liquid receipts are improved, reduce tail oil amount, technological process is simple, the operating of high conversion rate, device is stable.
2. anthracene oil hydrogenation method provided by the invention, hydrofinishing product is entered into high pressure hot separator, is separated into heat
High score vapour and hot high score oil；Hot high score vapour enters cold high pressure separator, is separated into refined cold gas separated by high pressure separator and refined cold high score oil；Heat
High score oil enters thermal low-pressure separators, is separated into refined low point of gas of heat and refined hot low point of oil；Hydrofinishing and it is hydrocracked
Hydrogen gas circulating system is using in parallel, hydrofining reactor entrance and the recycle hydrogen control of hydrofining reactor catalyst bed interlayer
Reactor inlet hydrogen-oil ratio and reactor catalyst bed interlayer temperature processed, suppress reactor temperature runaway；And disappear in hydrogenation process
The hydrogen of consumption, filled into by being hydrocracked section, can improve and be hydrocracked hydrogen purity in section hydrogen gas circulating system, improve and be hydrocracked
The hydrogen dividing potential drop of unit；In combination with the condition of accurate hydrofinishing and hydrocracking reaction (hydrogen-oil ratio, reaction temperature etc.), carry
High reaction depth and hydrogenation effect.
Brief description of the drawings
, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical scheme of the prior art
The required accompanying drawing used is briefly described in embodiment or description of the prior art, it should be apparent that, in describing below
Accompanying drawing is some embodiments of the present invention, for those of ordinary skill in the art, before creative work is not paid
Put, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the hydrogen gas circulating system carbolineum hydrogenation plant flow chart of the present invention；
Wherein icon is 1- hydrofining reactors, 2- hydrocracking reactors, 3- circulating hydrogen compressors, the new hydrogen pressures of 4-
Contracting machine, 5- high pressure hot separators, 6- thermal low-pressure separators, 7- cold high pressure separators, 8- cracking cold high pressure separators, 9- cold lows
Separator, 10- fractionating columns.
Embodiment
Embodiments of the present invention are sketched with reference to device flow chart.
Embodiment 1
The present embodiment is refined and is hydrocracked series connection using fixed bed hydrogenation, is refined with the hydrogen gas circulating system of cracking simultaneously
Connection, the PROCESS FOR TREATMENT carbolineum that new hydrogen is filled into by cracking zone are tested.
Process flow diagram is as shown in Figure 1：By carbolineum, pressurization, heating mix with entrance hydrogen after low point of oil dilution of heat, enter
Enter hydrofining reactor 1；Hot low point of oil as dilution can be the hot low point of oil or production of driving for the first time stored in advance
The hot low point of oil of raw storage, is waited after starting the cycle over, and low point of oil of heat is refined hot low point of oil.
The hydrofinishing product come out from finishing reactor bottom is after taking heat, into high pressure hot separator 5, separation
For hot high score vapour and hot high score oil.Hot high score vapour, into cold high pressure separator 7, is separated into refined after taking heat, note desalted water
Cold gas separated by high pressure separator and refined cold high score oil；After the oil decompression of hot high score, into thermal low-pressure separators 6, be separated into refined low point of gas of heat and
Low point of oil of refined heat.New hydrogen boosts to 18.3MPa (G) through make-up hydrogen compressor 4 and mixed with cracking entrance hydrogen as mixing hydrogen, mixing
After hydrogen is mixed with refined hot low point of oil by certain volume hydrogen-oil ratio, into cracker 2, injection recycle hydrogen control refining catalytic
Agent and Cracking catalyst bed temperature.The hydrocracking reaction product come out from cracker bottom flows through cracking cold anticyclone
Separator 8, it is separated into the cold gas separated by high pressure separator of cracking, the cold high score oil of cracking.
Mixed using the cold gas separated by high pressure separator of cracking with cold refined gas separated by high pressure separator deliver to circulating hydrogen compressor boost to 18.3MPa as circulation
Hydrogen；Recycle hydrogen carries out hydrofinishing, hydrocracking reaction as extraordinary hydrogen.
The cold high score oil of cracking is with after refined cold high score oil decompression, into cold low separator, being separated into cold low point of gas (fuel
Gas), cold low point of oil.Cold low point of oil is fractionated into tower 10 and is cut into naphtha cut, fuel oil, fuel gas and tail oil.Tail oil can be with
The low point of oil mixing preheating of the refined heat in part, is recycled to hydrofining reactor 1.
Wherein, the condition of hydrofining reaction be gross pressure be 18MPa, normal volume hydrogen-oil ratio be 800:1st, reaction temperature
For 350 DEG C, volume space velocity 1.0h-1, the composition and property of Hydrobon catalyst are：Molybdenum oxide 22wt%, nickel oxide
8wt%, carrier are aluminum oxide.Catalyst pore volume is 0.40ml/g, specific surface area 150m2/ g, catalyst amount are 80 μ g/g.
Hydrocracking reaction total system pressure is 18MPa, reaction temperature is 260 DEG C, reaction velocity 1.0h-1, standard body
Product hydrogen-oil ratio 2000:1, Cracking catalyst is 3976 catalyst.
Embodiment 2
The present embodiment is refined and is hydrocracked series connection using fixed bed hydrogenation, refines and cracking hydrogen gas circulating system is in parallel,
Different from embodiment 1 to be filled into respectively by cracking zone and exquisite section for new hydrogen, other parts are identical with such as embodiment 1.
Wherein, the condition of hydrofining reaction be gross pressure be 18MPa, normal volume hydrogen-oil ratio be 800:1st, reaction temperature
For 350 DEG C, volume space velocity 1.0h-1, the composition and property of Hydrobon catalyst are：Molybdenum oxide 22wt%, nickel oxide
8wt%, carrier are aluminum oxide.Catalyst pore volume is 0.40ml/g, specific surface area 150m2/ g, catalyst amount are 80 μ g/g.
Hydrocracking reaction total system pressure is 18MPa, reaction temperature is 260 DEG C, reaction velocity 1.0h-1, standard body
Product hydrogen-oil ratio 2000:1, Cracking catalyst is 3976 catalyst.
Embodiment 3
The present embodiment is refined and is hydrocracked series connection using fixed bed hydrogenation, refines and cracking hydrogen gas circulating system is connected,
The PROCESS FOR TREATMENT carbolineum that new hydrogen is filled into by refining stage is tested, different from embodiment 1 to make for the refined cold gas separated by high pressure separator of hydrofinishing
Hydrocracking reaction is carried out to be hydrocracked the recycle hydrogen of section, does not introduce new hydrogen, the cold gas separated by high pressure separator of cracking zone is through circulating hydrogen compressed
Machine boost cycle, other parts are identical with such as embodiment 1.
Wherein, the condition of hydrofining reaction be gross pressure be 18MPa, normal volume hydrogen-oil ratio be 800:1st, reaction temperature
For 350 DEG C, volume space velocity 1.0h-1, the composition and property of Hydrobon catalyst are：Molybdenum oxide 22wt%, nickel oxide
8wt%, carrier are aluminum oxide.Catalyst pore volume is 0.40ml/g, specific surface area 150m2/ g, catalyst amount are 80 μ g/g.
Hydrocracking reaction total system pressure is 18MPa, reaction temperature is 260 DEG C, reaction velocity 1.0h-1, standard body
Product hydrogen-oil ratio 2000:1, Cracking catalyst is 3976 catalyst.
The property of test raw material carbolineum used in embodiment 1-3 is as shown in table 1.Oxygen content is in carbolineum as shown in Table 1
1.5wt%, tenor is very low, gum level 22.94wt%, carbon residue 0.75wt%, sulphur and nitrogen content be 0.7wt%,
1wt%.The recycle hydrogen composition of reaction system is as shown in table 2, from Table 2, it can be seen that the hydrogen of the cracking zone in embodiment 1-3
Purity is respectively 97.57%, 92.71% and 89.21%.If hydrogenation system stagnation pressure is identical, hydrogenation reactor entrance hydrogen dividing potential drop
Sequence is embodiment 1>Embodiment 2>Embodiment 3, hydrogenation reaction depth can be improved, improve product liquid receipts and quality.It is logical
Comparative analysis table 3-4 is crossed, adjustment hydrofinishing fills into difference, embodiment 1-3 productions with being hydrocracked hydrogen gas circulating system and new hydrogen
It is respectively 95.6%, 88.2% and 85.1% that product liquid, which receives (it is liquefied gas, naphtha and fuel oil yield summation that liquid, which is received), and tail oil
Amount is respectively 2%, 10% and 14%.Meanwhile the excellent order of the product index such as content and Cetane number of sulphur and nitrogen is embodiment 1
>Embodiment 2>Embodiment 3.
In summary, the anthracene oil hydrogenation method of the present patent application, in the case where meeting refining stage hydrogen purity and hydrogen dividing potential drop, tune is passed through
Whole refine fills into the hydrogen gas circulating system of cracking and new hydrogen, heightens the hydrogen purity and hydrogen dividing potential drop of cracking zone, can increase reaction
Depth, product liquid receipts and quality are improved, reduces tail oil amount.
The property of the test raw material carbolineum of table 1
| Analysis project | Carbolineum | Limit value |
| Density (20 DEG C), kgm-3 | 1131 | ≯1200 |
| Elementary analysis | ||
| Sulphur, μ gg-1 | 7000 | |
| Nitrogen, μ gg-1 | 10000 | ≯12000 |
| Carbon, % | 91.32 | |
| Hydrogen, % | 5.48 | |
| Oxygen, % | 1.50 | |
| Boiling range (ASTM D86), DEG C | ||
| IBP/10% | 244/311 | IBP≮200 |
| 30%/50% | 332/349 | 50% ≯ 360 |
| 70%/90% | 372/411 | |
| 95%/EBP | 430/477 | 95% ≯ 460 |
| Free water, % | Vestige | <0.03 |
| Chlorine, ppm | 9 | ≯15 |
| Carbon residue, % | 0.75 | ≯1.7 |
| Flash-point (is remained silent), DEG C | 176 | |
| Four components, % | ||
| Saturation point | 2.72 | |
| Fragrance point | 73.70 | |
| Colloid | 22.94 | |
| Asphalitine | 0.64 | ≯1.0 |
| Metal, μ gg-1 | ≯30 | |
| Fe | 10.24 | ≯20 |
| Na+Ca | 0 | ≯10 |
The recycle hydrogen composition of the hydrogenation reaction system of table 2
The hydrogenation reaction product of 3 embodiment of table 1~3 is distributed
| Title | Embodiment 1 | Embodiment 2 | Embodiment 3 |
| Dry gas | 2.4 | 1.8 | 0.9 |
| Liquefied gas | 1 | 0.7 | 0.6 |
| Naphtha | 20.4 | 16.6 | 19.4 |
| Fuel oil | 74.2 | 70.9 | 65.1 |
| Tail oil | 2 | 10 | 14 |
The hydrogenated products property of 4 embodiment of table 1~3
Claims (10)
1. a kind of anthracene oil hydrogenation method, comprises the following steps：
(1) by the low point of oil dilution of carbolineum heat；
(2) carbolineum after step (1) is diluted mixes with entrance hydrogen, and it is anti-to carry out hydrofinishing under Hydrobon catalyst effect
Should, obtain hydrofinishing product；
(3) it is the hydrofinishing product obtained by step (2) is oily, refined through the refined cold gas separated by high pressure separator of separation acquisition, refined cold high score
Low point of gas of heat and refined hot low point of oil；
Specially：Hydrofinishing product is entered into high pressure hot separator, is separated into hot high score vapour and hot high score oil；Hot high score vapour
Into cold high pressure separator, refined cold gas separated by high pressure separator and refined cold high score oil are separated into；Hot high score oil enters thermal low-pressure separators, point
From for refined low point of gas of heat and refined hot low point of oil；
(4) the refined hot low point of oil in part is mixed with entrance hydrogen, then after filling into new hydrogen, carried out in the case where hydrocracking catalyst acts on
Hydrocracking reaction, obtain hydrocracking reaction product；
(5) separation is carried out to hydrocracking reaction product and obtains the cold gas separated by high pressure separator of cracking and the cold high score oil of cracking；By the cold height of cracking
Divide oil with carrying out separating to obtain cold low point of gas and cold low point of oil after the refined cold high score oil mixing in step (3)；
(6) by the cold low point of oil obtained by step (5), it is fractionated, obtains the various products for including tail oil；
Wherein, the pressure of the entrance hydrogen is 18.3MPa, includes the component of following molar percentage：H2S 1.00-1.13%,
NH30.85-0.91%, H294.20-94.39% and CH42.50-2.68%.
2. anthracene oil hydrogenation method according to claim 1, it is characterised in that by the cold gas separated by high pressure separator of cracking with refining cold gas separated by high pressure separator
Mixing delivers to circulating hydrogen compressor and boosts to 18.3MPa as recycle hydrogen；The recycle hydrogen is as hydrofining reactor and adds
The entrance hydrogen of the cold hydrogen of hydrogen cracker beds, hydrofinishing and hydrocracking reaction.
3. anthracene oil hydrogenation method according to claim 1 or 2, it is characterised in that the condition of hydrofinishing in step (2)
For：Reaction gross pressure is 18MPa, and normal volume hydrogen-oil ratio is 800~1500m3/m3, reaction temperature is 300 DEG C~450 DEG C, body
Product air speed is 0.1~5.0h-1。
4. anthracene oil hydrogenation method according to claim 2, it is characterised in that catalysis is set in the hydrofining reactor
Agent bed, is respectively provided with cold hydrogen inlet between catalyst bed top and bed, beds filling hydrogenation catalyst is described to add
The metallic compound that the active component of hydrogen catalyst is VI B and group VIII is one or more of, carrier is silica or oxidation
Aluminium；The catalyst pore volume is 0.20~0.50ml/g, 100~200m of specific surface area2/ g, catalyst charge are calculated as with metal
50~200 μ g/g.
5. anthracene oil hydrogenation method according to claim 4, it is characterised in that the active component content of the catalyst is：
Vib metals content is calculated as 5wt%~25wt% with metal oxide, and group VIII tenor is calculated as with metal oxide
1wt%~10wt%.
6. anthracene oil hydrogenation method according to claim 2, it is characterised in that in step (4), what hydrocracking reaction used
Reactor is air-liquid parallel type fixed bed reactors；Reaction condition is：Reaction temperature is 260~340 DEG C, and reaction gross pressure is
18MPa, reaction velocity are 0.1~4.0h-1, normal volume hydrogen-oil ratio is 1000~3000m3/m3。
7. the anthracene oil hydrogenation method according to claim 2 or 6, it is characterised in that the hydrocracking reactor top and
Cold hydrogen inlet is respectively provided between each beds, and loads Cracking catalyst；In Cracking catalyst, active material is
One or more in the oxide of cobalt, molybdenum or nickel, carrier are aluminum oxide, sieve and silica-sesquioxide or molecular sieve.
8. according to the anthracene oil hydrogenation method described in claim 1,2,4,5 or 6, it is characterised in that refined low point of the heat in the part
Oil is recycled to hydrofinishing section as carbolineum flux oil；The tail oil is recycled to hydrofinishing section as carbolineum flux oil.
9. anthracene oil hydrogenation method according to claim 3, it is characterised in that the refined hot low point of oil in the part, which is recycled to, to be added
Hydrogen refining stage is as carbolineum flux oil；The tail oil is recycled to hydrofinishing section as carbolineum flux oil.
10. anthracene oil hydrogenation method according to claim 7, it is characterised in that the refined hot low point of oil in the part is recycled to
Hydrofinishing section is as carbolineum flux oil；The tail oil is recycled to hydrofinishing section as carbolineum flux oil.
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106221792A (en) * | 2016-08-29 | 2016-12-14 | 山东恒信科技发展有限公司 | A kind of anthracene oil hydrogenation method |
| CN106281439A (en) * | 2016-08-29 | 2017-01-04 | 山东恒信科技发展有限公司 | A kind of method of producing light fuel oil by hydrogenating anthracene oil |
| CN106635154A (en) * | 2016-08-29 | 2017-05-10 | 山东恒信科技发展有限公司 | Anthracene oil hydrocracking method |
| CN109762595B (en) * | 2019-01-23 | 2020-12-01 | 上海众炅新能源科技有限公司 | Low-fused-ring-number coal-based anthracene oil and low-temperature-resistant coal-based fuel oil containing same |
| CN111871333B (en) * | 2020-07-16 | 2023-06-27 | 南京延长反应技术研究院有限公司 | Micro-interface reaction system and method for anthracene oil hydrogenation |
| CN111871332A (en) * | 2020-07-16 | 2020-11-03 | 南京延长反应技术研究院有限公司 | Reaction system and method for anthracene oil hydrogenation |
| CN115678593B (en) * | 2022-10-31 | 2024-06-25 | 山东恒信科技发展有限公司 | Coal tar anthracene oil hydrocracking process |
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| US8591726B2 (en) * | 2010-06-30 | 2013-11-26 | Exxonmobil Research And Engineering Company | Two stage hydroprocessing with divided wall column fractionator |
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| CN102851071A (en) * | 2012-08-27 | 2013-01-02 | 王小英 | Two-stage hydrogenation process of coal tar |
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