CN106281449B - A kind of method and system of coal tar production light Fuel and needle coke - Google Patents
A kind of method and system of coal tar production light Fuel and needle coke Download PDFInfo
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- CN106281449B CN106281449B CN201610902143.0A CN201610902143A CN106281449B CN 106281449 B CN106281449 B CN 106281449B CN 201610902143 A CN201610902143 A CN 201610902143A CN 106281449 B CN106281449 B CN 106281449B
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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 31
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000000446 fuel Substances 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 62
- 239000000047 product Substances 0.000 claims abstract description 58
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 38
- 239000000463 material Substances 0.000 claims abstract description 27
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 238000004939 coking Methods 0.000 claims abstract description 23
- 239000001257 hydrogen Substances 0.000 claims abstract description 20
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 20
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000000746 purification Methods 0.000 claims abstract description 19
- 239000012263 liquid product Substances 0.000 claims abstract description 18
- 239000000725 suspension Substances 0.000 claims abstract description 15
- 238000004821 distillation Methods 0.000 claims abstract description 14
- 230000003111 delayed effect Effects 0.000 claims abstract description 13
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 12
- 239000002283 diesel fuel Substances 0.000 claims abstract description 7
- 238000001914 filtration Methods 0.000 claims abstract description 7
- 230000000694 effects Effects 0.000 claims abstract description 3
- 238000002156 mixing Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 9
- 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
- 239000007787 solid Substances 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
- 150000002751 molybdenum Chemical class 0.000 claims description 3
- 150000003657 tungsten Chemical class 0.000 claims description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 239000011707 mineral Substances 0.000 claims description 2
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [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
- 239000000843 powder Substances 0.000 claims 1
- 238000007670 refining Methods 0.000 claims 1
- 239000003921 oil Substances 0.000 description 42
- 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
- 238000000926 separation method Methods 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
- 229910052759 nickel Inorganic materials 0.000 description 4
- 241000772415 Neovison vison Species 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur 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
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- 239000007809 chemical reaction catalyst Substances 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
- 239000000203 mixture Substances 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
- 229910000863 Ferronickel Inorganic materials 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
- 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
- 239000000428 dust Substances 0.000 description 1
- 238000000605 extraction Methods 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
- 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
- C10G67/14—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
Abstract
The present invention relates to the method and system that a kind of coal tar produces light Fuel and needle coke.The method of the present invention includes the following steps：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 and carries out hydrocracking reaction, obtain crackate；Step B, by the isolated cracked gas product of the crackate and hydrocracked liquid product, the hydrocracked liquid product is obtained by filtration oil phase and contains oil residue；Step C, the oil phase, hydrogen are sent into hydrofining reactor, carrying out hydrofining reaction under Hydrobon catalyst effect obtains processed gas product and purification product；Step D, the described purification product distillation, obtains naphtha cut, diesel oil distillate, heavy end；Step E, the heavy end is sent into delayed coking reaction tower, needle coke is prepared.The comprehensive utilization of coal tar can be achieved in the present invention, while significantly improving the economy of the technique.
Description
Technical field
The present invention relates in coal chemical technology more particularly to a kind of coal tar 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 set pyrolysis of coal unit scale 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
The coal tar of mostly middle coalite tar, property and conventional coking output has 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 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
The separation of hot high score obtains heavy residual stocks and light oil, and gas phase obtains liquid phase through low point of separation of heat, the low liquid separation phase of heat and distillation light oil (≤
320 DEG C or≤350 DEG C) extractant of the mixing as above-mentioned heavy residual stocks, light oil and residue oil are isolated in the second separator, the
Filtering obtains liquid phase after the mixing of light oil that one separator and the second separator are isolated, liquid phase again through distillation obtain light oil, in
Matter oil and mink cell focus, light oil and middle matter oil produce gasoline and aviation kerosine as hydrofinishing raw material, and mink cell focus is as delay
Coking raw material produces needle coke, and coking liquid phase is fed as slurry bed system hydrogenation reaction.But light oil is to the extraction efficiency of heavy residual stocks
It is limited, hetero atoms and the trace meters such as a large amount of sulphur, nitrogen can be contained in the mink cell focus obtained through distillation, directly as life
The raw material for producing needle coke, can seriously affect the quality of needle coke.
Invention content
The present invention is difficult to handle dusty, high metal, high-sulfur, high nitrogen, high resin and asphalt content for the prior art
Fast pyrogenation coal tar defect, it is proposed that the method and system of a kind of coal tar production light Fuel and needle coke make fast
Speed heat solution coal tar is comprehensively utilized.
The invention discloses a kind of methods that coal tar produces light Fuel and needle coke, and the method includes following steps
Suddenly：
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 oil phase and contains oil residue；
Step C, the oil phase, hydrogen are sent into hydrofining reactor, are carried out under Hydrobon catalyst effect
Hydrofining reaction obtains processed gas product and purification product；
Step D, the described purification product distillation, obtains naphtha cut, diesel oil distillate, heavy end；
Step E, the heavy end is sent into delayed coking reaction tower, needle coke is prepared.
In the above-mentioned method for producing light Fuel and needle coke by coal tar, while obtaining needle coke in the step E
Coking oil can be also obtained, the coking oil is used for the charging of hydrofining reaction in step C.
In the above-mentioned method for producing light Fuel and needle coke by coal tar, the suspension bed hydrogenation catalyst is heterogeneous
Mineral dust.
In the above-mentioned method for producing light Fuel and needle coke by coal tar, the suspension bed hydrogenation catalyst is yellow iron
One or more of mine, red mud, bloodstone, josephinite, limonite, inorganic molybdenum salt, inorganic tungsten salt.
In the above-mentioned method for producing light Fuel and needle coke by coal tar, the hydrocracking reaction pressure is 14~
26MPa, preferably 16~24MPa；The hydrocracking reaction temperature is 390~500 DEG C, preferably 400~470 DEG C；It is described
The percentage that suspension bed hydrogenation catalyst accounts for the mixed material is 0.1~5wt%.
In the above-mentioned method for producing light Fuel and needle coke by coal tar, the Hydrobon catalyst in the step C
In one or more of containing Ni, Mo, W, carrier is γ-Al2O3。
In the above-mentioned method for producing light Fuel and needle coke by coal tar, the hydrofining reaction pressure is 8~
15MPa；The hydrofining reaction temperature is 380~440 DEG C；Volume space velocity is when liquid during the hydrofining reaction
0.5~2.0h-1；The percent by volume of the hydrogen and the oil phase is (600~1200):1.
The invention also discloses a kind of system producing light Fuel and needle coke for above-mentioned coal tar, the system packets
Include sequentially connected blending tank, floating bed hydrogenation reactor, the first separator, filter, hydrofining reactor, the second separation
Device, atmospheric distillation tower, delayed coking reaction tower；
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；
There is the filter hydrocracked liquid product entrance, oil phase to export, the hydrocracked liquid product entrance and described first
The hydrocracked liquid product outlet connection of separator；
The hydrofining reactor have oil phase entrance, hydrogen inlet, refined products outlet, the oil phase entrance with it is described
The oil phase outlet connection of 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 tower have heavy end entrance, needle coke export, the heavy end entrance with it is described often
Press the heavy end outlet connection of distiller.
Further, the filter also has oil-containing solid discharge.
Further, the delayed coking reaction tower also has coking oil export.
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 it is effectively improved the product of needle coke
Matter, realizes the comprehensive utilization of coal tar, while significantly improving the economy of the technique.
Description of the drawings
Fig. 1 is the system schematic that coal tar produces light Fuel and needle coke in the embodiment of the present invention.
Fig. 2 is the method flow schematic diagram that coal tar produces light Fuel and needle coke in the embodiment of the present invention.
Reference numeral in attached 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.
Specific implementation mode
Below in conjunction with drawings and examples, the specific implementation mode 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
It applies example to be for illustrative purposes only, rather than limiting the invention.
As shown in Figure 1, it is the system schematic of coal tar production light Fuel and needle coke in the embodiment of the present invention.This is
System includes sequentially connected blending tank 1, floating bed hydrogenation reactor 2, the first separator 3, filter 4, hydrofining reactor
5, the second separator 6, atmospheric distillation tower 7, delayed coking reaction tower 8.The specific connection relation between each device carries out below
Detailed introduction.
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.
Filter 4 has hydrocracked liquid product entrance, oil phase outlet, oil-containing solid discharge.Wherein, hydrocracked liquid product enters
The hydrocracked liquid product of mouth and the first separator 3, which exports, to be connected.
Hydrofining reactor 5 has oil phase entrance, hydrogen inlet, refined products outlet.Wherein, oil phase entrance and filtering
The oil phase outlet connection of device 4.
Second separator 6 has refined products entrance, processed gas product exit, purification product exit.Wherein, 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 tower 8 has heavy end entrance, needle coke outlet, coking oil export.Wherein, heavy end enters
The heavy end of mouth and air-distillation device 7, which exports, to be connected.
Based on above system, the invention also provides a kind of methods that coal tar produces light Fuel and needle coke.Fig. 2 is
For the idiographic flow schematic diagram of this method.
As shown in Figure 2, the method for coal tar production light Fuel and needle coke proposed by the present invention, includes the following steps：
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 being passed through hydrogen thereto via hydrogen inlet so that mixed
It closes material and carries out hydrocracking reaction 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 mine, 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 being 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 respectively via cracked gas product outlet, the first separator 3 of hydrocracked liquid product outlet discharge.Then, by cracked liquid
After collection of products, via hydrocracked liquid product entrance be sent into filter 4 in, be obtained by filtration oil phase, contain oil residue, and respectively via
Oil phase outlet, oil-containing solid discharge discharge filter 4.
Step C, hydrofining reaction：The oil phase being discharged in above-mentioned steps B is sent into hydrofining reaction via oil phase entrance
In device 5, meanwhile, it is passed through hydrogen via hydrogen inlet, wherein under the action of Hydrobon catalyst, it is anti-to carry out hydrofinishing
It answers.Refined products are obtained after reaction, and export discharge hydrofining reactor 5 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.
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 when liquid in reaction process-1, the percent by volume of hydrogen and oil phase is (600
~1200):1.
Wherein, when liquid volume space velocity be air speed a kind of representation.In the embodiment of the present invention, volume space velocity refers to when liquid
It is the volume that unit volume Hydrobon catalyst handles oil phase per hour.
Step D, light Fuel is produced：The purification product being discharged in above-mentioned steps C is via purification product inlet
It is sent into atmospheric distillation tower 7, naphtha cut, diesel oil distillate, heavy end is obtained after distillation, and respectively via naphtha cut
Outlet, diesel oil distillate outlet, heavy end outlet discharge atmospheric distillation tower 7.Wherein, naphtha cut, diesel oil distillate are this
Light Fuel needed for invention.
Step E, needle coke is prepared：The heavy end being discharged in above-mentioned steps D is sent into delay coke via heavy end entrance
Change in reaction tower 8, carries out delayed coking reaction and needle coke, coking oil is prepared, and respectively via needle coke outlet, coking oil
Outlet discharge delayed coking reaction tower 8.Wherein, charging of the coking oil for hydrofining reaction in step C.
Embodiment 1
The catalyst choice josephinite (iron content 48.5wt%, nickeliferous 1.5wt%) that floating bed hydrogenation reacts in the present embodiment,
Grain size is 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.
The active component of hydrofining reaction catalyst selects Ni, W composition metal, 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 when 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.
Raw material in the present embodiment once passes through, charging of the coking oil not as hydrofining reaction.What embodiment 1 used
The main character of fast pyrogenation coal tar is shown in Table 1, and obtained primary product distribution is shown in Table 2.
Embodiment 2
The additive amount of the catalyst choice nitric acid molybdenum that floating bed hydrogenation reacts in the present embodiment, 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.
The active component of hydrofining reaction catalyst selects Ni, W, Mo composition metal, 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 when 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.
Raw material in the present embodiment once passes through, charging of the coking oil not as hydrofining reaction.What embodiment 1 used
The main character of fast pyrogenation coal tar 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
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 of coal tar production light Fuel and needle coke, which is characterized in that the described method comprises the following steps：
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 oil phase and contains oil residue；
Step C, the oil phase, hydrogen are sent into hydrofining reactor, carry out adding hydrogen under Hydrobon catalyst effect
Refining reaction obtains processed gas product and purification product；
Step D, the described purification product distillation, obtains naphtha cut, diesel oil distillate, heavy end；
Step E, the heavy end is sent into delayed coking reaction tower, needle coke is prepared.
2. according to the method described in claim 1, can also be obtained while it is characterized in that, obtaining needle coke in the step E
Coking oil, the coking oil are used for the charging of hydrofining reaction in step C.
3. according to the method described in claim 1, it is characterized in that, the suspension bed hydrogenation catalyst is heterogeneous mineral powder
End.
4. 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.
5. according to the method described in claim 1, it is characterized in that,
The hydrocracking reaction pressure is 14~26MPa；
The hydrocracking reaction temperature is 390~500 DEG C；
The percentage that the suspension bed hydrogenation catalyst accounts for the mixed material is 0.1~5wt%.
6. according to the method described in claim 5, it is characterized in that,
The hydrocracking reaction pressure is 16~24MPa；
The hydrocracking reaction temperature 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 hydrofining reaction pressure is 8~15MPa；
The hydrofining reaction temperature is 380~440 DEG C；
Volume space velocity is 0.5~2.0h when liquid during the hydrofining reaction-1；
The percent by volume of the hydrogen and the oil phase is (600~1200):1.
9. a kind of system producing light Fuel and needle coke according to any methods of claim 1-8, which is characterized in that
The system comprises sequentially connected blending tank, floating bed hydrogenation reactor, the first separator, filter, hydrofining reactions
Device, the second separator, atmospheric distillation tower, delayed coking reaction tower；
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；
There is the filter hydrocracked liquid product entrance, oil phase to export, which detaches with described first
The hydrocracked liquid product outlet connection of device；
The hydrofining reactor has oil phase entrance, hydrogen inlet, refined products outlet, the oil phase entrance and the filtering
The oil phase outlet connection of device；
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；
There is the delayed coking reaction tower heavy end entrance, needle coke to export, which steams with the normal pressure
Evaporate the heavy end outlet connection of device.
10. system according to claim 9, which is characterized in that the filter also has oil-containing solid discharge.
11. system according to claim 9, which is characterized in that the 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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| CN101302443B (en) * | 2008-06-20 | 2011-05-18 | 中国石油大学(华东) | Combined process for cogeneration of needle coke and light oil |
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