CN106281449A - A kind of coal tar produces light Fuel and the method and system of needle coke - Google Patents
A kind of coal tar produces light Fuel and the method and system of needle coke Download PDFInfo
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- CN106281449A CN106281449A CN201610902143.0A CN201610902143A CN106281449A CN 106281449 A CN106281449 A CN 106281449A CN 201610902143 A CN201610902143 A CN 201610902143A CN 106281449 A CN106281449 A CN 106281449A
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- 239000011280 coal tar Substances 0.000 title claims abstract description 49
- 239000011331 needle coke Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000000446 fuel Substances 0.000 title claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 62
- 239000000047 product Substances 0.000 claims abstract description 60
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 40
- 239000000463 material Substances 0.000 claims abstract description 27
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- 238000004939 coking Methods 0.000 claims abstract description 26
- 238000000746 purification Methods 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 19
- 239000012263 liquid product Substances 0.000 claims abstract description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000001257 hydrogen Substances 0.000 claims abstract description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 18
- 239000000725 suspension Substances 0.000 claims abstract description 16
- 230000003111 delayed effect Effects 0.000 claims abstract description 14
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 10
- 239000002283 diesel fuel Substances 0.000 claims abstract description 7
- 230000000694 effects Effects 0.000 claims abstract description 4
- 238000002156 mixing Methods 0.000 claims description 12
- 238000004821 distillation Methods 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- 229910052721 tungsten Inorganic materials 0.000 claims description 5
- 229910003158 γ-Al2O3 Inorganic materials 0.000 claims description 5
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 3
- 238000001914 filtration Methods 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
- 150000003657 tungsten Chemical class 0.000 claims description 3
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical group [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 2
- 229910052683 pyrite Inorganic materials 0.000 claims description 2
- 239000011028 pyrite Substances 0.000 claims description 2
- 238000005336 cracking Methods 0.000 claims 1
- 238000001704 evaporation Methods 0.000 claims 1
- 229910052742 iron Inorganic materials 0.000 claims 1
- 239000000843 powder Substances 0.000 claims 1
- 238000007670 refining Methods 0.000 claims 1
- 239000003921 oil Substances 0.000 description 43
- 239000012071 phase Substances 0.000 description 21
- 239000003245 coal Substances 0.000 description 15
- 239000002994 raw material Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 238000000197 pyrolysis Methods 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 241000772415 Neovison vison Species 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 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
- 239000010426 asphalt Substances 0.000 description 2
- 239000007809 chemical reaction catalyst Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000010586 diagram 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
- 230000035484 reaction time Effects 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910000863 Ferronickel Inorganic materials 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
- 230000007547 defect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 125000005842 heteroatom Chemical group 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
- 238000003672 processing method Methods 0.000 description 1
- 238000000926 separation method Methods 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
- C10G67/14—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 at least two different refining steps in the absence of hydrogen
-
- 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
- C10G2300/201—Impurities
- C10G2300/205—Metal content
- C10G2300/206—Asphaltenes
-
- 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)
- Coke Industry (AREA)
Abstract
The present invention relates to a kind of coal tar and produce light Fuel and the method and system of needle coke.The method of the present invention comprises the following steps: step A, coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, and described mixed material feeding floating bed hydrogenation reactor is carried out hydrocracking reaction, obtains crackate；Step B, by described crackate isolated cracked gas product and hydrocracked liquid product, described hydrocracked liquid product is filtrated to get oil phase and containing oil residue；Step C, described oil phase, hydrogen are sent in hydrofining reactor, under Hydrobon catalyst effect, carry out hydrofining reaction obtain processed gas product and purification product；Step D, described purification product distill, and obtain naphtha cut, diesel oil distillate, heavy end；Step E, by described heavy end send into delayed coking reaction tower, prepare needle coke.The present invention can realize the comprehensive utilization of coal tar, significantly improves the economy of this technique simultaneously.
Description
Technical field
The present invention relates in coal chemical technology, particularly relate to a kind of coal tar produce light Fuel and the method for needle coke and
System.
Background technology
It is considered as to realize the effective way that Coal Clean efficiently utilizes that coal sub-prime utilizes, Ye Shi China " 13 " coal
The direction that chemical industry is given priority to.The sub-prime of coal utilizes and is through being pyrolyzed to enter the coal gas in coal, coal tar and semicoke etc.
Row separates.Wherein, coal tar can produce gasoline, diesel oil by hydrogenation, semicoke by pyrolysis become low volatile, low-sulfur clear
Clean fuel or raw material.
To extract the coal tar oil and gas of scale production quantities, coal sub-prime utilizes to be needed to realize scale, maximization.Coal heat
" leading " that solution technology utilizes as coal sub-prime, wherein, single set pyrolysis of coal unit scale is more and more large-scale, and pyrolysis rate
Improving the most rapidly, the coal time of staying in pyrolysis oven is only several seconds, and it is fast that pyrolysis oil gas overflows speed, and the coal tar of output
Mostly being middle coalite tar, its character has bigger difference with the coal tar of conventional coking output.
Fine coal carries out the coal tar of middle low-temperature rapid thermal solution generation and mostly is oil under water, containing substantial amounts of coal dust and coal in tar
Ash, gum asphaltic content is high, and viscosity is relatively big, and water content is higher, and heat stability is poor.Especially in the low crude oil price epoch,
Fast pyrogenation coal tar is carried out the deep processing of high-efficiency and economic, the economy important in inhibiting that coal sub-prime is utilized.Cause
This, the research to coal tar processing method is of increased attention.
Prior art one discloses a kind of coal tar hydrogenation process maximally utilizing coal tar residue, and this technique is to steam
Evaporate the heavy distillat (> 320 DEG C obtained or > 350 DEG C) use slurry bed system hydrogenation reactor to carry out hydrogenation reaction, hydrogenation products liquid phase warp
Hot high score separates and obtains heavy residual stocks and light oil, and gas phase separates through low point of heat and obtains liquid phase, hot low separatory phase and distillation light oil (≤
320 DEG C or≤350 DEG C) mix the extractant as above-mentioned heavy residual stocks, the second separator is isolated light oil and residue oil, the
One separator and the second separator isolated light oil mixing after filter obtain liquid phase, liquid phase again through distillation obtain light oil, in
Matter oil and mink cell focus, light oil and middle matter oil are as hydrofinishing raw material production gasoline and aerial kerosene, and mink cell focus is as delay
Coking raw material produces needle coke, and coking liquid phase feeds as slurry bed system hydrogenation reaction.But, the light oil extraction efficiency to heavy residual stocks
Limited, the hetero atoms such as substantial amounts of sulfur, nitrogen, and trace meter can be contained in the mink cell focus that distillation obtains, it is directly as life
Produce the raw material of needle coke, the quality of needle coke can be had a strong impact on.
Summary of the invention
The present invention is directed to prior art be difficult to process high dust, high metal, high-sulfur, high nitrogen, high resin and asphalt content
The defect of fast pyrogenation coal tar, it is proposed that a kind of coal tar produces light Fuel and the method and system of needle coke, makes fast
Speed pyrolyzing coal tar obtains comprehensive utilization.
The invention discloses a kind of coal tar and produce light Fuel and the method for needle coke, described method includes following step
Rapid:
Step A, coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, and described mixed material is sent into
Floating bed hydrogenation reactor carries out hydrocracking reaction, obtains crackate；
Step B, by described crackate isolated cracked gas product and hydrocracked liquid product, described cracked liquid produces
Thing is filtrated to get oil phase and containing oil residue；
Step C, described oil phase, hydrogen are sent in hydrofining reactor, carry out under Hydrobon catalyst effect
Hydrofining reaction obtains processed gas product and purification product；
Step D, described purification product distill, and obtain naphtha cut, diesel oil distillate, heavy end；
Step E, by described heavy end send into delayed coking reaction tower, prepare needle coke.
In the above-mentioned method being produced light Fuel and needle coke by coal tar, while described step E obtains needle coke
Also can obtain coking oil, described coking oil is the charging of hydrofining reaction in step C.
In the above-mentioned method being produced light Fuel and needle coke by coal tar, described suspension bed hydrogenation catalyst is heterogeneous
Mineral dust.
In the above-mentioned method being produced light Fuel and needle coke by coal tar, described suspension bed hydrogenation catalyst is yellow ferrum
One or more in ore deposit, red mud, bloodstone, josephinite, limonite, inorganic molybdenum salt, inorganic tungsten salt.
In the above-mentioned method being produced light Fuel and needle coke by coal tar, described hydrocracking reaction pressure be 14～
26MPa, preferably 16～24MPa；Described hydrocracking reaction temperature is 390～500 DEG C, preferably 400～470 DEG C；Described
It is 0.1～5wt% that suspension bed hydrogenation catalyst accounts for the percentage ratio of described mixed material.
In the above-mentioned method being produced light Fuel and needle coke by coal tar, the Hydrobon catalyst in described step C
In containing one or more in Ni, Mo, W, carrier is γ-Al2O3。
In the above-mentioned method being produced light Fuel and needle coke by coal tar, described hydrofining reaction pressure be 8～
15MPa；Described hydrofining reaction temperature is 380～440 DEG C；During described hydrofining reaction, during liquid, volume space velocity is
0.5～2.0h-1；Described hydrogen is (600～1200) with the percent by volume of described oil phase: 1.
The invention also discloses a kind of for above-mentioned coal tar production light Fuel and the system of needle coke, described system bag
Include be sequentially connected with blending tank, floating bed hydrogenation reactor, the first separator, filter, hydrofining reactor, second separate
Device, atmospheric distillation tower, delayed coking reaction tower；
Described blending tank has coal tar entrance, suspension bed hydrogenation catalyst entrance, mixed material outlet；
Described floating bed hydrogenation reactor has mixed material entrance, hydrogen inlet, crackate outlet, this mixed material
Entrance exports with the mixed material of described blending tank and is connected；
Described first separator has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet, and this splits
Change product inlet to be connected with the crackate outlet of described floating bed hydrogenation reactor；
Described filter has hydrocracked liquid product entrance, oil phase outlet, this hydrocracked liquid product entrance and described first
The hydrocracked liquid product outlet of separator connects；
Described hydrofining reactor has oil phase entrance, hydrogen inlet, refined products outlet, and this oil phase entrance is with described
The oil phase outlet of filter connects；
Described second separator has refined products entrance, processed gas product exit, purification product exit, this essence
Product inlet processed exports with the refined products of described hydrofining reactor and is connected；
Described atmospheric distillation tower has purification product inlet, naphtha cut outlet, diesel oil distillate exports, heavy evaporates
Separating mouth, this purification product inlet is connected with the purification product exit of described second separator；
Described delayed coking reaction tower have heavy end entrance, needle coke outlet, this heavy end entrance with described often
The heavy end outlet of pressure distillator connects.
Further, described filter also has oil-containing solid discharge.
Further, described delayed coking reaction tower also has coking oil export.
The present invention can utilize high dust, high metal, high-sulfur, high nitrogen, the quick coal pyrolyzing of high resin and asphalt content
Tar, produces light Fuel and needle coke.
As the heavy end of production needle-shape coke raw material, the present invention can effectively remove the colloid in this heavy end, drip
Blue or green matter, metal and sulfur, and improve four PAHs and the content of five PAHs in needle coke, and then it is effectively improved the product of needle coke
Matter, it is achieved the comprehensive utilization of coal tar, significantly improves the economy of this technique simultaneously.
Accompanying drawing explanation
Fig. 1 is that in the embodiment of the present invention, coal tar produces light Fuel and the system schematic of needle coke.
Fig. 2 is that in the embodiment of the present invention, coal tar produces light Fuel and the method flow schematic diagram of needle coke.
Reference in accompanying drawing is as follows:
1, blending tank；2, floating bed hydrogenation reactor；3, the first separator；4, filter；5, hydrofining reactor；6、
Second separator；7, atmospheric distillation tower；8, delayed coking reaction tower.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and its various aspects.But, specific embodiments described below and reality
Executing example is only descriptive purpose rather than limitation of the present invention.
As shown in Figure 1, light Fuel and the system schematic of needle coke are produced for coal tar in the embodiment of the present invention.This is
Blending tank 1 that system includes being sequentially connected with, floating bed hydrogenation reactor the 2, first separator 3, filter 4, hydrofining reactor
5, the second separator 6, atmospheric distillation tower 7, delayed coking reaction tower 8.Hereinafter the concrete annexation between each device is carried out
Detailed introduction.
Blending tank 1 has coal tar entrance, suspension bed hydrogenation catalyst entrance, mixed material outlet.
Floating bed hydrogenation reactor 2 has mixed material entrance, hydrogen inlet, crackate outlet.Wherein, mixed material
Entrance exports with the mixed material of blending tank 1 and is connected.
First separator 3 has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet.Wherein, split
Change product inlet to be connected with the crackate outlet of floating bed hydrogenation reactor 2.
Filter 4 has hydrocracked liquid product entrance, oil phase outlet, oil-containing solid discharge.Wherein, hydrocracked liquid product enters
Mouth exports with the hydrocracked liquid product of the first separator 3 and is connected.
Hydrofining reactor 5 has oil phase entrance, hydrogen inlet, refined products outlet.Wherein, oil phase entrance and filtration
The oil phase outlet of device 4 connects.
Second separator 6 has refined products entrance, processed gas product exit, purification product exit.Wherein, essence
Product inlet processed exports with the refined products of hydrofining reactor 5 and is connected.
Atmospheric distillation tower 7 has purification product inlet, naphtha cut outlet, diesel oil distillate outlet, heavy end
Outlet.Wherein, the purification product exit of purification product inlet and the second separator 6 connects.
Delayed coking reaction tower 8 has heavy end entrance, needle coke outlet, coking oil export.Wherein, heavy end enters
Mouth exports with the heavy end of air-distillation device 7 and is connected.
Based on said system, the invention allows for a kind of coal tar and produce light Fuel and the method for needle coke.Fig. 2 is i.e.
Idiographic flow schematic diagram for the method.
As shown in Figure 2, the coal tar that the present invention proposes produces light Fuel and the method for needle coke, comprises the steps:
Step A, being hydrocracked of coal tar: coal tar is carried out dehydrate, and it is miscellaneous to remove bulky grain machinery therein
Matter, purifies coal tar, then itself and suspension bed hydrogenation catalyst is urged via coal tar entrance, floating bed hydrogenation respectively
Agent entrance is sent in blending tank 1, obtains mixed material after mix homogeneously.After the blended material outlet of mixed material is discharged, warp
Sent in floating bed hydrogenation reactor 2 by mixed material entrance.Meanwhile, hydrogen it is passed through wherein via hydrogen inlet so that mixed
Compound material carries out hydrocracking reaction in floating bed hydrogenation reactor 2, and the crackate obtained after reaction is via crackate
Outlet is discharged.
Wherein, suspension bed hydrogenation catalyst selects heterogeneous mineral dust, specially pyrite, red mud, bloodstone, ferronickel
One or more in ore deposit, limonite, inorganic molybdenum salt, inorganic tungsten salt.Further, the addition of this suspension bed hydrogenation catalyst accounts for mixed
The percentage ratio of compound material is 0.1～5wt% (wt% is mass percent).
In this step, the mixed material of coal tar and suspension bed hydrogenation catalyst enters in floating bed hydrogenation reactor 2
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 send via crackate entrance
Enter in the first separator 3.In the first separator 3, crackate carries out isolated cracked gas product, cracked liquid produces
Thing, and discharge the first separator 3 via cracked gas product outlet, hydrocracked liquid product outlet respectively.Then, by cracked liquid
After product collection, send in filter 4 via hydrocracked liquid product entrance, be filtrated to get oil phase, containing oil residue, and respectively via
Oil phase outlet, oil-containing solid discharge discharge filter 4.
Step C, hydrofining reaction: the oil phase discharged in above-mentioned steps B sends into hydrofining reaction via oil phase entrance
In device 5, meanwhile, it is passed through hydrogen via hydrogen inlet, wherein under the effect of Hydrobon catalyst, carries out hydrofinishing anti-
Should.Obtain refined products after reaction, and discharge hydrofining reactor 5 via refined products outlet.After refined products is discharged, warp
Sent in the second separator 6 by refined products entrance, after separation, obtain processed gas product, purification product, and warp respectively
The second separator 6 is discharged by processed gas product exit, purification product exit.
Wherein, the hydrogenation active component in Hydrobon catalyst is one or more in Ni, Mo, W, and the present invention implements
Carrier in example selects γ-Al2O3。
In this step, the reaction condition carrying out hydrofining reaction is: reaction pressure is 8～15MPa, and reaction temperature is
380～440 DEG C, during liquid in course of reaction, volume space velocity is 0.5～2.0h-1, hydrogen is (600 with the percent by volume of oil phase
～1200): 1.
Wherein, during liquid, volume space velocity is a kind of representation of air speed.In the embodiment of the present invention, during liquid, volume space velocity refers to
It it is the unit volume Hydrobon catalyst volume that processes oil phase per hour.
Step D, production light Fuel: the purification product discharged in above-mentioned steps C is via purification product inlet
Send in atmospheric distillation tower 7, after distillation, obtain naphtha cut, diesel oil distillate, heavy end, and respectively via naphtha cut
Atmospheric distillation tower 7 is discharged in outlet, diesel oil distillate outlet, heavy end outlet.Wherein, naphtha cut, diesel oil distillate are this
Light Fuel needed for invention.
Step E, prepare needle coke: the heavy end discharged in above-mentioned steps D sends into delay coke via heavy end entrance
Change in reaction tower 8, carry out delayed coking reaction and prepare needle coke, coking oil, and respectively via needle coke outlet, coking oil
Delayed coking reaction tower 8 is discharged in outlet.Wherein, coking oil charging of hydrofining reaction in step C.
Embodiment 1
The catalyst choice josephinite (iron content 48.5wt%, nickeliferous 1.5wt%) of floating bed hydrogenation reaction in the present embodiment,
Particle diameter is 100～200 mesh, and addition is 1.5wt%.The reaction condition of hydrocracking reaction is: reaction pressure is 18MPa, instead
Answering temperature is 440 DEG C.
The active component of hydrofining reaction catalyst selects Ni, W composition metal, wherein NiO and WO3Content be respectively
4.1wt%, 18.7wt%, carrier is γ-Al2O3.The reaction condition of hydrofining reaction is: reaction pressure is 10MPa, reaction
Temperature is 400 DEG C, and during liquid, volume space velocity is 1.0h-1, hydrogen is 800:1 with the percent by volume of oil phase.
The condition of delayed coking reaction is: reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
Raw material in the present embodiment once passes through, and coking oil is not as the charging of hydrofining reaction.Embodiment 1 uses
The main character of fast pyrogenation coal tar is shown in Table 1, and the primary product distribution obtained is shown in Table 2.
Embodiment 2
The catalyst choice nitric acid molybdenum of floating bed hydrogenation reaction in the present embodiment, the addition of this catalyst is 0.5wt%
(by the content meter of Mo element), the reaction condition of hydrocracking reaction is: reaction pressure is 22MPa, and reaction temperature is 460 DEG C.
The active component of hydrofining reaction catalyst selects Ni, W, Mo composition metal, wherein NiO, MoO, WO3Content
Being respectively 4.1wt%, 5.2wt%, 20.7wt%, carrier is γ-Al2O3.The reaction condition of hydrofining reaction is: reaction pressure
Power is 12MPa, and reaction temperature is 420 DEG C, and during liquid, volume space velocity is 1.5h-1, hydrogen is 1000:1 with the percent by volume of oil phase.
The condition of delayed coking reaction is: reaction temperature is 450 DEG C, and the isothermal reaction time is 9h.
Raw material in the present embodiment once passes through, and coking oil is not as the charging of hydrofining reaction.Embodiment 1 uses
The main character of fast pyrogenation coal tar is shown in Table 1, and the primary product distribution obtained is shown in Table 2.
The main character of table 1 fast pyrogenation coal tar
Table 2 embodiment 1 and the distribution of embodiment 2 primary product
Shown in Tables 1 and 2, the operating condition of embodiment 1 and embodiment 2 can realize the comprehensive utilization of fast pyrogenation coal tar
With, produce light Fuel and the needle coke with industrial application value.
It is last that it is noted that obviously above-described embodiment is only for clearly demonstrating example of the present invention, and also
The non-restriction to embodiment.For those of ordinary skill in the field, can also do on the basis of the above description
Go out change or the variation of other multi-form.Here without also cannot all of embodiment be given exhaustive.And thus drawn
What Shen went out obviously changes or changes among still in protection scope of the present invention.
Claims (10)
1. a coal tar produces light Fuel and the method for needle coke, it is characterised in that said method comprising the steps of:
Step A, coal tar and suspension bed hydrogenation catalyst are mixed to get mixed material, and described mixed material is sent into suspend
Bed hydroprocessing reactor carries out hydrocracking reaction, obtains crackate；
Step B, by described crackate isolated cracked gas product and hydrocracked liquid product, described hydrocracked liquid product mistake
Filter obtains oil phase and containing oil residue；
Step C, described oil phase, hydrogen are sent in hydrofining reactor, be hydrogenated with under Hydrobon catalyst effect
Refining reaction obtains processed gas product and purification product；
Step D, described purification product distill, and obtain naphtha cut, diesel oil distillate, heavy end；
Step E, by described heavy end send into delayed coking reaction tower, prepare needle coke.
Method the most according to claim 1, it is characterised in that also can obtain while obtaining needle coke in described step E
Coking oil, described coking oil is the charging of hydrofining reaction in step C.
Method the most according to claim 1, it is characterised in that described suspension bed hydrogenation catalyst is heterogeneous mineral powder
End.
Method the most according to claim 1, it is characterised in that described suspension bed hydrogenation catalyst is pyrite, red mud, red
One or more in iron mine, josephinite, limonite, inorganic molybdenum salt, inorganic tungsten salt.
Method the most according to claim 1, it is characterised in that
Described hydrocracking reaction pressure is 14～26MPa, preferably 16～24MPa；
Described hydrocracking reaction temperature is 390～500 DEG C, preferably 400～470 DEG C；
It is 0.1～5wt% that described suspension bed hydrogenation catalyst accounts for the percentage ratio of described mixed material.
Method the most according to claim 1, it is characterised in that in the Hydrobon catalyst in described step C containing Ni,
One or more in Mo, W, carrier is γ-Al2O3。
Method the most according to claim 1, it is characterised in that
Described hydrofining reaction pressure is 8～15MPa；
Described hydrofining reaction temperature is 380～440 DEG C；
During described hydrofining reaction, during liquid, volume space velocity is 0.5～2.0h-1；
Described hydrogen is (600～1200) with the percent by volume of described oil phase: 1.
8. producing light Fuel and a system for needle coke for the coal tar that one of claim 1-7 is described, its feature exists
The blending tank that includes being sequentially connected with in, described system, floating bed hydrogenation reactor, the first separator, filter, hydrofinishing are anti-
Answer device, the second separator, atmospheric distillation tower, delayed coking reaction tower；
Described blending tank has coal tar entrance, suspension bed hydrogenation catalyst entrance, mixed material outlet；
Described floating bed hydrogenation reactor has mixed material entrance, hydrogen inlet, crackate outlet, this mixed material entrance
Export with the mixed material of described blending tank and be connected；
Described first separator has crackate entrance, cracked gas product outlet, hydrocracked liquid product outlet, and this cracking is produced
Thing entrance exports with the crackate of described floating bed hydrogenation reactor and is connected；
Described filter has hydrocracked liquid product entrance, oil phase outlet, and this hydrocracked liquid product entrance separates with described first
The hydrocracked liquid product outlet of device connects；
Described hydrofining reactor has oil phase entrance, hydrogen inlet, refined products outlet, this oil phase entrance and described filtration
The oil phase outlet of device connects；
Described second separator has refined products entrance, processed gas product exit, purification product exit, this refined product
Thing entrance exports with the refined products of described hydrofining reactor and is connected；
Described atmospheric distillation tower has purification product inlet, naphtha cut outlet, diesel oil distillate exports, heavy end goes out
Mouthful, this purification product inlet is connected with the purification product exit of described second separator；
Described delayed coking reaction tower has heavy end entrance, needle coke outlet, and this heavy end entrance steams with described normal pressure
The heavy end outlet evaporating device connects.
System the most according to claim 8, it is characterised in that described filter also has oil-containing solid discharge.
System the most according to claim 8, it is characterised in that described delayed coking reaction tower also has coking oil export.
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| CN110938461A (en) * | 2018-09-23 | 2020-03-31 | 何巨堂 | Suspension bed hydrogenation modification method of coal tar containing coal pitch |
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