CN106281447B - A kind of coal tar maximizes the method and system of production light Fuel and needle coke - Google Patents
A kind of coal tar maximizes the method and system of production light Fuel and needle coke Download PDFInfo
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- CN106281447B CN106281447B CN201610902769.1A CN201610902769A CN106281447B CN 106281447 B CN106281447 B CN 106281447B CN 201610902769 A CN201610902769 A CN 201610902769A CN 106281447 B CN106281447 B CN 106281447B
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- 239000011280 coal tar Substances 0.000 title claims abstract description 46
- 239000011331 needle coke Substances 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000000446 fuel Substances 0.000 title claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 239000000047 product Substances 0.000 claims abstract description 65
- 239000000463 material Substances 0.000 claims abstract description 41
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 40
- 238000004939 coking Methods 0.000 claims abstract description 37
- 239000007791 liquid phase Substances 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 27
- 239000007789 gas Substances 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000012071 phase Substances 0.000 claims abstract description 22
- 238000000746 purification Methods 0.000 claims abstract description 20
- 239000012263 liquid product Substances 0.000 claims abstract description 18
- 239000000725 suspension Substances 0.000 claims abstract description 16
- 230000003111 delayed effect Effects 0.000 claims abstract description 15
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 13
- 239000002283 diesel fuel Substances 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 8
- 238000010411 cooking Methods 0.000 claims abstract description 5
- 230000000694 effects Effects 0.000 claims abstract description 4
- 238000004821 distillation Methods 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 8
- 229910052721 tungsten Inorganic materials 0.000 claims description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 229910003158 γ-Al2O3 Inorganic materials 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 3
- 239000011707 mineral Substances 0.000 claims description 3
- 150000002751 molybdenum Chemical class 0.000 claims description 3
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 3
- 229910052683 pyrite Inorganic materials 0.000 claims description 3
- 239000011028 pyrite Substances 0.000 claims description 3
- 150000003657 tungsten Chemical class 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 238000005336 cracking Methods 0.000 claims 1
- 239000000843 powder Substances 0.000 claims 1
- 238000007670 refining Methods 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 47
- 239000003245 coal Substances 0.000 description 16
- 239000002994 raw material Substances 0.000 description 6
- 238000000197 pyrolysis Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 241000772415 Neovison vison Species 0.000 description 3
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000011269 tar Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000007809 chemical reaction catalyst Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910000863 Ferronickel Inorganic materials 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 210000004556 brain Anatomy 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- DBRMBYFUMAFZOB-UHFFFAOYSA-N molybdenum nitric acid Chemical compound [Mo].[N+](=O)(O)[O-] DBRMBYFUMAFZOB-UHFFFAOYSA-N 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
- 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
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0409—Extraction of unsaturated hydrocarbons
- C10G67/0445—The hydrotreatment being a hydrocracking
-
- 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
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0409—Extraction of unsaturated hydrocarbons
- C10G67/0418—The hydrotreatment being a hydrorefining
-
- 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
-
- 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
- C10G2400/06—Gasoil
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to the method and system that coal tar maximizes production light Fuel and needle coke.The present invention includes：Coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, mixed material is sent into floating bed hydrogenation reactor carries out hydrocracking reaction, obtains crackate；By the isolated cracked gas product of crackate and hydrocracked liquid product, hydrocracked liquid product is obtained by filtration liquid phase and containing oil residue；Liquid phase, hydrogen are sent into hydrofining reactor, hydrofining reaction is carried out under Hydrobon catalyst effect, refined products, isolated processed gas product and purification product are obtained, purification product distills to obtain naphtha cut, diesel oil distillate, heavy end；Heavy end is sent into delayed coking reaction device, obtains needle coke, cooking gas, coking liquid；It coking liquid and is mixed containing oil residue, oil phase and residue is obtained by filtration.The achievable coal tar of the present invention maximally utilizes, and with preferably economic benefit.
Description
Technical field
The present invention relates to the sides that coal chemical technology more particularly to a kind of coal tar maximize production light Fuel and needle coke
Method and system.
Background technology
The utilization of coal sub-prime is considered as the effective way and China " 13 " coal that realization Coal Clean efficiently utilizes
The direction that chemical industry is given priority to.The sub-prime of coal using be exactly by be pyrolyzed by coal gas, coal tar and semicoke in coal etc. into
Row separation.Wherein, coal tar can produce gasoline, diesel oil by adding hydrogen, semicoke by pyrolysis become low volatile, low-sulfur it is clear
Clean fuel or raw material.
To extract the coal tar oil and gas of scale production quantities, coal sub-prime, which utilizes, to be needed to realize scale, enlargement.Coal heat
" tap " that solution technology is utilized as coal sub-prime, wherein, single pyrolysis of coal unit scale that covers is more and more large-scale, and pyrolysis rate
Also rapid to improve, residence time of the coal in pyrolysis oven is only several seconds, and pyrolysis oil gas spilling speed is fast, and the coal tar of output
Mostly middle coalite tar, the coal tar of property and conventional coking output have bigger difference.
The coal tar that low-temperature rapid thermal solution generates during fine coal carries out is mostly underwater oil, contains a large amount of coal dust and coal in tar
Ash, gum asphaltic content is high, and viscosity is larger, and water content is higher, and thermal stability is poor.Especially in the low crude oil price epoch,
The deep processing of high-efficiency and economic, the economy important in inhibiting utilized for coal sub-prime are carried out to fast pyrogenation coal tar.Cause
This, it is of increased attention to the research of coal tar processing method.
The prior art one discloses a kind of coal tar hydrogenation process for maximally utilizing coal tar oil residue, which is that will steam
Evaporate heavy distillat (>320 DEG C or>350 DEG C) using slurry bed system hydrogenation reactor progress hydrogenation reaction, hydrogenation products liquid phase warp
Hot high score separation obtains heavy residual stocks and light oil, and gas phase separately wins to obtain light oil through heat is low, this two parts light oil and distillation light oil (≤320
DEG C or≤350 DEG C) extractant of the mixing as above-mentioned heavy residual stocks, obtain liquid phase after filtering, liquid phase is again through distillation acquisition lightweight
Oily, middle matter oil and mink cell focus, light oil and middle matter oil produce gasoline and aviation kerosine, mink cell focus conduct as hydrofinishing raw material
Delayed coking raw material produces needle coke, and coking liquid phase is fed as slurry bed system hydrogenation reaction.But extraction of the light oil to heavy residual stocks
Limited efficacy can contain hetero atoms and the trace meters such as a large amount of sulphur, nitrogen through distilling, directly make in the mink cell focus obtained
To produce the raw material of needle coke, the quality of needle coke can be seriously affected.
Invention content
The present invention is intended to provide a kind of coal tar maximizes the method and system of production light Fuel and needle coke.The present invention
Maximizing is utilized containing oil residue so that the coal tar of coal fast pyrogenation process generation is comprehensively utilized, and improve economic effect
Benefit.
The present invention proposes a kind of method that coal tar maximizes production light Fuel and needle coke, the method includes with
Lower step：
Step A, coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, and the mixed material is sent into
Floating bed hydrogenation reactor carries out hydrocracking reaction, obtains crackate；
Step B, by the isolated cracked gas product of the crackate and hydrocracked liquid product, the cracked liquid production
Object is obtained by filtration liquid phase and containing oil residue；
Step C, the liquid phase, hydrogen are sent into hydrofining reactor, are carried out under Hydrobon catalyst effect
Hydrofining reaction, obtains refined products, the isolated processed gas product of the refined products and purification product, described
Purification product distills to obtain naphtha cut, diesel oil distillate, heavy end；
Step D, the heavy end is sent into delayed coking reaction device, needle coke, cooking gas, coking liquid is obtained by the reaction
Body；
Step E, it by being mixed containing oil residue in the coking liquid and the step B, is then obtained by filtration
Oil phase and residue.
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the suspension bed hydrogenation catalyst is
Heterogeneous mineral dust.
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the suspension bed hydrogenation catalyst is
One or more of pyrite, red mud, bloodstone, josephinite, limonite, inorganic molybdenum salt, inorganic tungsten salt.
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the suspension in the step A
The percentage that bed hydrogenation catalyst accounts for the mixed material is 0.1~5wt%.
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the pressure of the hydrocracking reaction
For 14~26MPa, preferably 16~24MPa；The temperature of the hydrocracking reaction be 390~500 DEG C, preferably 400~470
℃。
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the hydrofinishing in the step C
Containing one or more of Ni, Mo, W in catalyst, carrier is γ-Al2O3。
In the above-mentioned method that production light Fuel and needle coke are maximized by coal tar, the pressure of the hydrofining reaction
For 8~15MPa, temperature is 380~440 DEG C；Volume space velocity is 0.5~2.0h during liquid during the hydrofining reaction-1；Institute
The percent by volume for stating hydrogen and the liquid phase is (600~1200):1.
It is described the invention also provides a kind of system that production light Fuel and needle coke are maximized for above-mentioned coal tar
System includes blending tank, floating bed hydrogenation reactor, the first separator, first filter, hydrofining reactor, the second separation
Device, atmospheric distillation tower, delayed coking reaction device, washing tank, the second filter；
The blending tank has coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material outlet；
The floating bed hydrogenation reactor has mixed material entrance, hydrogen inlet, crackate outlet, the mixed material
The mixed material outlet of entrance and the blending tank connects；
First separator has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet, this splits
The crackate outlet for changing product inlet and the floating bed hydrogenation reactor connects；
The first filter have hydrocracked liquid product entrance, liquid-phase outlet, the hydrocracked liquid product entrance with it is described
The hydrocracked liquid product outlet connection of first separator；
The hydrofining reactor have liquid phase entrance, hydrogen inlet, refined products outlet, the liquid phase entrance with it is described
The liquid-phase outlet connection of first filter；
Second separator has refined products entrance, processed gas product exit, purification product exit, the essence
The refined products outlet of product inlet processed and the hydrofining reactor connects；
There is the atmospheric distillation tower purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy to evaporate
Sub-export, the purification product inlet are connect with the purification product exit of second separator；
The delayed coking reaction utensil has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid discharge
Mouthful, the heavy end outlet of the heavy end entrance and the air-distillation device connects；
The washing tank have coking liquid inlet, oil-containing residue entrance, mixed material outlet, the coking liquid inlet with
The coking liquid outlet connection of the delayed coking reaction device；
Second filter has mixed material entrance, and the mixed material entrance and the mixed material of the washing tank go out
Mouth connection.
Further, the first filter also has oil-containing solid discharge.
Further, second filter also has oil phase outlet and solid discharge, oil phase outlet and described plus hydrogen
The liquid phase entrance connection of finishing reactor.
The present invention can utilize the quick coal pyrolyzing of dusty, high metal, high-sulfur, high nitrogen, high resin and asphalt content
Tar, to produce light Fuel and needle coke.
As the heavy end of production needle-shape coke raw material, the present invention can effectively remove colloid in the heavy end, drip
Green matter, metal and sulphur, and the content of four cycloaromatics and five cycloaromatics in needle coke is improved, and then be effectively improved the product of needle coke
Matter.
Achievable the maximally utilizing containing oil residue of the present invention.Coking liquid is as the extractant containing oil residue, Ke Yichong
Divide and recycle containing the oil phase in oil residue, which can be used as hydrofining reaction to feed, so as to significantly improve light fraction yield,
The economy of the technique is improved simultaneously.
Description of the drawings
Fig. 1 is the system schematic that coal tar maximizes production light Fuel and needle coke in the embodiment of the present invention.
Fig. 2 is the method flow schematic diagram that coal tar maximizes production light Fuel and needle coke in the embodiment of the present invention.
Reference numeral in attached drawing is as follows：
1st, blending tank；2nd, floating bed hydrogenation reactor；3rd, the first separator；4th, first filter；5th, hydrofining reaction
Device；6th, the second separator；7th, atmospheric distillation tower；8th, delayed coking reaction device；9th, washing tank；10th, the second filter.
Specific embodiment
Below in conjunction with drawings and examples, the specific embodiment of the present invention is described in more details, so as to energy
The advantages of enough more fully understanding the solution of the present invention and its various aspects.However, specific embodiments described below and reality
Example is applied to be for illustrative purposes only rather than limitation of the present invention.
As shown in Figure 1, the system signal of production light Fuel and needle coke is maximized for coal tar in the embodiment of the present invention
Figure.The system includes sequentially connected blending tank 1, floating bed hydrogenation reactor 2, the first separator 3, first filter 4 plus hydrogen
Finishing reactor 5, the second separator 6, atmospheric distillation tower 7, delayed coking reaction device 8, washing tank 9, the second filter 10.Below
Specific connection relation between each device is described in detail.
Blending tank 1 has coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material outlet.
Floating bed hydrogenation reactor 2 has mixed material entrance, hydrogen inlet, crackate outlet.Wherein, mixed material
The mixed material outlet of entrance and blending tank 1 connects.
First separator 3 has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet.Wherein, it splits
The crackate outlet for changing product inlet and floating bed hydrogenation reactor 2 connects.
First filter 4 has hydrocracked liquid product entrance, liquid-phase outlet, oil-containing solid discharge.Wherein, cracked liquid produces
The hydrocracked liquid product of object entrance and the first separator 3 outlet connection.
Hydrofining reactor 5 has liquid phase entrance, hydrogen inlet, refined products outlet.Wherein, liquid phase entrance and first
The liquid-phase outlet connection of filter 4.
Second separator 6 has refined products entrance, processed gas product exit, purification product exit.Wherein, it is smart
The refined products outlet of product inlet processed and hydrofining reactor 5 connects.
Atmospheric distillation tower 7 has purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy end
Outlet.Wherein, purification product inlet is connect with the purification product exit of the second separator 6.
Delayed coking reaction device 8 has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid outlet.
Wherein, heavy end entrance and the heavy end outlet of air-distillation device 7 connect.
Washing tank 9 has coking liquid inlet, oil-containing residue entrance, mixed material outlet.Wherein, coking liquid inlet with
The coking liquid outlet connection of delayed coking reaction device 8, oil-containing residue entrance and the oil-containing solid discharge of first filter 4 connect
It connects.
Second filter 10 has mixed material entrance, oil phase outlet, solid discharge.Wherein, mixed material entrance is with washing
The mixed material outlet connection of tank 9 is washed, oil phase outlet is connect with the liquid phase entrance of hydrofining reactor 5.
Based on above system, the invention also provides a kind of coal tar maximizes the side of production light Fuel and needle coke
Method.Fig. 2 is the idiographic flow schematic diagram of this method.
As shown in Figure 2, the method that coal tar proposed by the present invention maximizes production light Fuel and needle coke, including as follows
Step：
Step A, coal tar is hydrocracked：Coal tar is dehydrated, and it is miscellaneous to remove bulky grain machinery therein
Matter purifies coal tar, then urges itself and suspension bed hydrogenation catalyst via coal tar oil-in, floating bed hydrogenation respectively
Agent entrance is sent into blending tank 1, obtains mixed material after mixing.Mixed material is after mixed material outlet discharge, warp
It is sent into floating bed hydrogenation reactor 2 by mixed material entrance.Meanwhile it is passed through hydrogen thereto via hydrogen inlet so that mixed
It closes material and hydrocracking reaction is carried out in floating bed hydrogenation reactor 2, the crackate obtained after reaction is via crackate
Outlet discharge.
Wherein, suspension bed hydrogenation catalyst selects heterogeneous mineral dust, specially pyrite, red mud, bloodstone, ferronickel
One or more of ore deposit, limonite, inorganic molybdenum salt, inorganic tungsten salt.Also, the additive amount of the suspension bed hydrogenation catalyst accounts for mixed
The percentage for closing material is 0.1~5wt% (wt% is mass percent).
In this step, the mixed material of coal tar and suspension bed hydrogenation catalyst in floating bed hydrogenation reactor 2 into
The reaction condition of row hydrocracking reaction is：Reaction pressure is 14~26MPa, preferably 16~24MPa；Reaction temperature is 390
~500 DEG C, preferably 400~470 DEG C.
Step B, the separating and filtering of crackate：The crackate discharged in above-mentioned steps A is sent via crackate entrance
Enter in the first separator 3.In the first separator 3, crackate carries out isolated cracked gas product, cracked liquid production
Object, and exported respectively via cracked gas product, the first separator 3 of hydrocracked liquid product outlet discharge.Then, by cracked liquid
It after collection of products, is sent into first filter 4 via hydrocracked liquid product entrance, liquid phase is obtained by filtration, containing oil residue, and respectively
Via liquid-phase outlet, oil-containing solid discharge discharge first filter 4.
Step C, light Fuel is produced：The liquid phase discharged in above-mentioned steps B is sent into hydrofining reaction via liquid phase entrance
In device 5, meanwhile, hydrogen is passed through via hydrogen inlet, wherein under the action of Hydrobon catalyst, it is anti-to carry out hydrofinishing
It should.Refined products are obtained after reaction, and discharge hydrofining reactor 5 is exported via refined products.After refined products discharge, warp
It is sent into the second separator 6 by refined products entrance, processed gas product, purification product is obtained after separation, and pass through respectively
Second separator 6 is discharged by processed gas product exit, purification product exit.
Above-mentioned purification product is sent into via purification product inlet in atmospheric distillation tower 7, and stone brain is obtained after distillation
Oil distillate, diesel oil distillate, heavy end, and exported respectively via naphtha cut, diesel oil distillate outlet, heavy end outlet row
Go out atmospheric distillation tower 7.Wherein, naphtha cut, diesel oil distillate are the required light Fuel of the present invention.
Wherein, the hydrogenation active component in Hydrobon catalyst is one or more of Ni, Mo, W, and the present invention is implemented
Carrier selection γ-Al in example2O3。
In this step, the reaction condition for carrying out hydrofining reaction is：Reaction pressure is 8~15MPa, and reaction temperature is
380~440 DEG C, volume space velocity is 0.5~2.0h during liquid in reaction process-1, the percent by volume of hydrogen and oil phase is (600
~1200):1.
Wherein, a kind of representation of the volume space velocity for air speed during liquid.In the embodiment of the present invention, volume space velocity refers to during liquid
It is the volume that unit volume Hydrobon catalyst handles oil phase per hour.
Step D, needle coke is prepared：The heavy end discharged in above-mentioned steps C is sent into delay coke via heavy end entrance
Change in reactor 8, carry out delayed coking reaction and needle coke, cooking gas, coking liquid is prepared, and respectively via needle coke
Outlet, cooking gas outlet, coking liquid outlet discharge delayed coking reaction device 8.
Step E, extraction is containing the oil phase in oil residue：The coking liquid discharged in above-mentioned steps D is via coking liquid inlet
It is sent into washing tank 9.Meanwhile in step B first filter 4 discharge be also fed into washing via oil-containing residue entrance containing oil residue
In tank 9.Coking liquid is sufficiently mixed in washing tank 9 and stirs to get mixed material as the extractant containing oil residue, and via
Mixed material outlet discharge washing tank 9.
Said mixture material is sent into via mixed material entrance in the second filter 10, oil phase, residue is obtained by filtration, and divide
It is not exported via oil phase, solid discharge discharges the second filter 10.
In the step, coking liquid can be recycled fully as the extractant containing oil residue containing the oil phase in oil residue.It is obtained
The oil phase obtained is sent into via the liquid phase entrance of hydrofining reactor 5 in hydrofining reactor 5, as hydrofining reaction
Charging, so as to significantly improve light fraction yield.
The residue that extraction process obtains in the step is used for metallurgical raw material.
Embodiment 1
The catalyst choice josephinite (iron content 48.5wt%, nickeliferous 1.5wt%) that floating bed hydrogenation reacts in the present embodiment,
Grain size be 100~200 mesh, additive amount 1.5wt%.The reaction condition of hydrocracking reaction is：Reaction pressure is 18MPa, instead
It is 440 DEG C to answer temperature.
Active component selection Ni, W composition metal of hydrofining reaction catalyst, wherein NiO and WO3Content be respectively
4.1wt%, 18.7wt%, carrier are γ-Al2O3.The reaction condition of hydrofining reaction is：Reaction pressure is 10MPa, reaction
Temperature is 400 DEG C, and volume space velocity is 1.0h during liquid-1, the percent by volume of hydrogen and oil phase is 800：1.
The condition of delayed coking reaction is：Reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
In the present embodiment, coking liquid is as the extractant containing oil residue, after being sufficiently mixed stirring in washing tank 9, warp
Second filter 10 filters to isolate oil phase and residue, and oil phase is smart together as hydrogen is added with the liquid phase that first filter 4 is isolated
Make the charging of reaction.
The main character for the fast pyrogenation coal tar that embodiment 1 uses is shown in Table 1, and obtained primary product distribution is shown in Table 2.
Embodiment 2
The catalyst choice nitric acid molybdenum that floating bed hydrogenation reacts in the present embodiment, the additive amount of the catalyst is 0.5wt%
(content meter for pressing Mo elements), the reaction condition of hydrocracking reaction is：Reaction pressure is 22MPa, and reaction temperature is 460 DEG C.
Active component selection Ni, W, Mo composition metal of hydrofining reaction catalyst, wherein NiO, MoO, WO3Content
Respectively 4.1wt%, 5.2wt%, 20.7wt%, carrier are γ-Al2O3.The reaction condition of hydrofining reaction is：Reaction pressure
Power is 12MPa, and reaction temperature is 420 DEG C, and volume space velocity is 1.5h during liquid-1, the percent by volume of hydrogen and oil phase is 1000：1.
The condition of delayed coking reaction is：Reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
In the present embodiment, coking liquid is as the extractant containing oil residue, after being sufficiently mixed stirring in washing tank 9, warp
Second filter 10 filters to isolate oil phase and residue, and oil phase is smart together as hydrogen is added with the liquid phase that first filter 4 is isolated
Make the charging of reaction.
The main character for the fast pyrogenation coal tar that embodiment 1 uses is shown in Table 1, and obtained primary product distribution is shown in Table 2.
The main character of 1 fast pyrogenation coal tar of table
2 embodiment 1 of table and the distribution of 2 primary product of embodiment
As shown in Tables 1 and 2, the operating condition of embodiment 1 and embodiment 2 can realize the comprehensive profit of fast pyrogenation coal tar
With producing light Fuel and needle coke with industrial application value.
Finally it should be noted that：Obviously, the above embodiment is merely an example for clearly illustrating the present invention, and simultaneously
The non-restriction to embodiment.For those of ordinary skill in the art, it can also do on the basis of the above description
Go out other various forms of variations or variation.There is no necessity and possibility to exhaust all the enbodiments.And thus drawn
The obvious changes or variations that Shen goes out are still in the protection scope of this invention.
Claims (11)
1. a kind of method that coal tar maximizes production light Fuel and needle coke, which is characterized in that the method includes following
Step：
Step A, coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, and the mixed material is sent into and is suspended
Bed hydroprocessing reactor carries out hydrocracking reaction, obtains crackate；
Step B, by the isolated cracked gas product of the crackate and hydrocracked liquid product, the hydrocracked liquid product mistake
Filter obtains liquid phase and containing oil residue；
Step C, the liquid phase, hydrogen are sent into hydrofining reactor, carry out adding hydrogen under Hydrobon catalyst effect
Refining reaction, obtains refined products, the isolated processed gas product of the refined products and purification product, described refined
Product liquid distills to obtain naphtha cut, diesel oil distillate, heavy end；
Step D, the heavy end is sent into delayed coking reaction device, needle coke, cooking gas, coking liquid is obtained by the reaction；
Step E, by being mixed containing oil residue in the coking liquid and the step B, oil phase is then obtained by filtration
And residue.
2. according to the method described in claim 1, it is characterized in that, the suspension bed hydrogenation catalyst is heterogeneous mineral powder
End.
3. according to the method described in claim 1, it is characterized in that, the suspension bed hydrogenation catalyst be pyrite, it is red mud, red
One or more of iron ore, josephinite, limonite, inorganic molybdenum salt, inorganic tungsten salt.
4. according to the method described in claim 1, it is characterized in that, the suspension bed hydrogenation catalyst in the step A accounts for
The percentage of the mixed material is 0.1~5wt%.
5. according to the method described in claim 1, it is characterized in that,
The pressure of the hydrocracking reaction is 14~26MPa；
The temperature of the hydrocracking reaction is 390~500 DEG C.
6. according to the method described in claim 5, it is characterized in that,
The pressure of the hydrocracking reaction is 16~24MPa；
The temperature of the hydrocracking reaction is 400~470 DEG C.
7. according to the method described in claim 1, it is characterized in that, in Hydrobon catalyst in the step C containing Ni,
One or more of Mo, W, carrier are γ-Al2O3。
8. according to the method described in claim 1, it is characterized in that,
The pressure of the hydrofining reaction is 8~15MPa, and temperature is 380~440 DEG C；
Volume space velocity is 0.5~2.0h during liquid during the hydrofining reaction-1；
The percent by volume of the hydrogen and the liquid phase is (600~1200):1.
9. a kind of system for maximizing production light Fuel and needle coke according to any methods of claim 1-8, special
Sign is that the system comprises blending tank, floating bed hydrogenation reactor, the first separator, first filter, hydrofining reactions
Device, the second separator, atmospheric distillation tower, delayed coking reaction device, washing tank, the second filter；
The blending tank has coal tar oil-in, suspension bed hydrogenation catalyst entrance, mixed material outlet；
The floating bed hydrogenation reactor has mixed material entrance, hydrogen inlet, crackate outlet, the mixed material entrance
It exports and connects with the mixed material of the blending tank；
First separator has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet, cracking production
Object entrance and the crackate outlet of the floating bed hydrogenation reactor connect；
The first filter has hydrocracked liquid product entrance, liquid-phase outlet, the hydrocracked liquid product entrance and described first
The hydrocracked liquid product outlet connection of separator；
The hydrofining reactor has liquid phase entrance, hydrogen inlet, refined products outlet, the liquid phase entrance and described first
The liquid-phase outlet connection of filter；
Second separator has refined products entrance, processed gas product exit, purification product exit, the refined production
Object entrance and the refined products outlet of the hydrofining reactor connect；
There is the atmospheric distillation tower purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy end to go out
Mouthful, which connect with the purification product exit of second separator；
The delayed coking reaction utensil has heavy end entrance, needle coke outlet, cooking gas outlet, coking liquid outlet,
The heavy end outlet of the heavy end entrance and the air-distillation device connects；
The washing tank have coking liquid inlet, oil-containing residue entrance, mixed material outlet, the coking liquid inlet with it is described
The coking liquid outlet connection of delayed coking reaction device；
Second filter has mixed material entrance, and the mixed material outlet of the mixed material entrance and the washing tank connects
It connects.
10. system according to claim 9, which is characterized in that the first filter also has oil-containing solid discharge.
11. system according to claim 9, which is characterized in that second filter also has oil phase outlet and residue
Outlet, oil phase outlet are connect with the liquid phase entrance of the hydrofining reactor.
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| CN101724419B (en) * | 2008-10-28 | 2013-05-01 | 中国石油化工股份有限公司 | Method for producing needle coke by utilizing delay coking of coal tar |
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