CN105950227A - Treatment system and method for pyrolyzed oil gas - Google Patents
Treatment system and method for pyrolyzed oil gas Download PDFInfo
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- CN105950227A CN105950227A CN201610514978.9A CN201610514978A CN105950227A CN 105950227 A CN105950227 A CN 105950227A CN 201610514978 A CN201610514978 A CN 201610514978A CN 105950227 A CN105950227 A CN 105950227A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- 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
- C10G2400/26—Fuel gas
Abstract
The invention discloses a treatment system and method for pyrolyzed oil gas. The treatment method comprises: preparing condensed heavy oil and cooled oil gas through the pyrolyzed oil gas under the spraying effect of cooling oil; distilling the cooled oil gas to obtain pyrolyzed gas and normal-pressure tower bottom heavy oil; generating a hydrogenation product by the tower bottom heavy oil under the action of a catalyst and hydrogen; separating the hydrogenation product to obtain cracked gas and cracked oil; decompressing and distilling the cracked oil to obtain quenched oil and decompressed tower bottom heavy oil; supplying the quenched oil to a quencher; carrying out gas separation on the cracked gas and the pyrolyzed gas to obtain hydrogen and fuel gas. The system comprises a gas separator, and the quencher, a normal-pressure distillation tower, a suspension bed hydrogenation reactor, a gas-liquid separator and a decompression distillation tower which are connected in sequence. According to the treatment system and method, a decompressed light fraction part of a hydrogenation product of a suspension bed for the pyrolyzed oil gas is used as a cooling medium of the pyrolyzed oil gas, and the pyrolyzed oil gas is primarily cooled, so that secondary condensation and coke production in a cooling process can be avoided, and the yield of light oil is improved.
Description
Technical field
The present invention relates to a kind of system and method by pyrolysis oil gas processing light-weight fuel oil.More
Saying of body, is during coal fast pyrogenation, the recovery of coupling pyrolysis oil gas and the course of processing, it is thus achieved that
The system and method for light-weight fuel oil.
Background technology
The utilization of coal sub-prime is considered as the effective way that Coal Clean efficiently utilizes, Ye Shi China " ten
Three or five " direction that Coal Chemical Industry is given priority to.The sub-prime of coal utilizes and is through pyrolysis by coal
In heterogeneity separate, including the coal gas finally given, tar and semicoke etc..Wherein, burnt
Oil can produce gasoline, diesel oil by hydrogenation, and semicoke becomes low volatile, low-sulfur by pyrolysis
Cleaning fuel, replaces dissipating the pollution burning coal minimizing to air.
" leading " that coal sub-prime utilizes is the pyrolytic technique of coal, pyrolytic technique scale production quantities to be extracted
Tar, coal gas.Along with the progress of science and technology, coal sub-prime utilizes scale, maximization, single set coal heat
Solving unit scale the most more and more large-scale, and pyrolysis rate improves the most rapidly, coal is in pyrolysis oven
The time of staying be only several seconds, it is fast that pyrolysis oil gas overflows speed, and the coal tar of output mostly be in low
Temperature coal tar, its character has bigger difference with the coal tar of conventional coking output.
In existing process of coking, coke-stove gas from carbonizing chamber tedge effusion temperature is
650～750 DEG C, first spraying the ammonia of 70～75 DEG C in bridge tube and discharge, coal gas is cooled to 80～85 DEG C,
In coal gas, the tar of 60% is cooled, and condense out is heavy tar, sprays ammonia and ensures tar stream
Dynamic property.The processing mode using this routine carrys out the pyrolysis oil that the coal fast pyrogenation for the treatment of scale produces
Gas, can consume substantial amounts of ammonia, and produce large amount of sewage；Although its light constituent content is higher than high-temperature coal
Tar, but fast pyrogenation coal tar contains more toluene insolubles, mainly coal dust and coal ash,
And viscosity compared with big, emulsifying degree high, heat stability is poor, difficulty of processing is big, needs appropriate design
Reclaim and processing scheme realizes comprehensive utilization, to increase economic efficiency.
Existing a kind of raw coke oven gas cooling fractional method and coking technology, will discharge from coke furnace carbonization chamber
Raw coke oven gas cools down in fractionating device step by step, proposes famine step by step according to fraction boiling point order from high to low
Different fractions in coal gas, fractionating device fractionate out the most successively Colophonium, anthracene oil, a carbolineum,
Washing oil and naphtalene oil, and subsequent recovery raw coke oven gas.This mode, directly enters the raw coke oven gas of 650～700 DEG C
Entering fractionating device, first fractionate out Colophonium bottom fractionating device, segregation apparatus bottom temp is higher,
The easy coking of asphalt component.Every grade of dephlegmator arranges dividing plate and only arranges protruding through hole in centre and can cause
Fractional distillation precision reduces, during in raw coke oven gas, the heavy constituent of non-total condensation can be brought into light component.In addition
Arranging spray thrower, reflux pump and temperature-adjusting device in every level shunt device, technique is complex, device
Long period stable operation be relatively difficult to ensure card, therefore, the method is unsuitable for the coal fast pyrolysis process of scale
The recovery of middle pyrolysis oil gas.
Separately have slurry bed system and fixed bed coupling process that a kind of full fraction of coal tar is hydrogenated with, the method be by
Pretreated coal tar carries out fractional distillation after slurry bed system is hydrocracked, and fractional distillation gained light components enters
Fixed bed hydrogenation refined unit, midbarrel and catalyst loop back slurry bed system hydrogenation reactor, heavy
Component returns tar pretreated unit circulation hydrogenation after partial catalyst and coke are removed by filtration.The party
Method is first to process, full fraction of coal tar for the middle low temperature coal tar more containing light components through slurry bed system
Oil, in slurry bed system hydrocracking process, gas phase hydrocarbon is more, and system pressure can be caused to raise, and hydrogen divides
Pressure drop is low, affects the conversion ratio of heavy component, causes waste.
Summary of the invention
The present invention, in order to adapt to the requirement of recovery and the processing being pyrolyzed oil gas in fast pyrolysis process, improves
Heavy component conversion ratio, it is to avoid coking, proposes a kind of processing system being pyrolyzed oil gas and processing method.
The present invention is to be achieved through the following technical solutions foregoing invention purpose:
A kind of processing system being pyrolyzed oil gas, including: quencher, it is provided with pyrolysis oil gas entrance, chilling
Oil-in, cooling oil gas vent and condensation heavy oil outlet；Atmospheric distillation tower, be provided with cooling oil gas entrance,
Pyrolysis gas outlet, quench oil entrance and heavy oil outlet；Described cooling oil gas entrance and described chilling
The cooling oil gas vent of device connects；Floating bed hydrogenation reactor, is provided with heavy oil entrance, hydrogenation products goes out
Mouth, hydrogen inlet；Described heavy oil entrance exports with the heavy oil of described atmospheric distillation tower and is connected；Gas-liquid is divided
From device, it is provided with hydrogenation products entrance, cracking gas exit and cracked oil outlet；Described hydrogenation products entrance
Export with the hydrogenation products of described floating bed hydrogenation reactor and be connected；Vacuum distillation tower, is provided with cracked oil
The outlet of entrance, quench oil and circulation heavy oil outlet；Described cracked oil entrance and described gas-liquid separator
Cracked oil outlet connects；The outlet of described quench oil is connected with the quench oil entrance of described quencher；Gas
Separator, is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen outlet；Described pyrolysis gas entrance and institute
The pyrolysis gas outlet stating atmospheric distillation tower connects；Described cracked gas entrance splits with described gas-liquid separator
Activating QI outlet connects.
Further, the condensation heavy oil of described quencher exports and described floating bed hydrogenation reactor
Heavy oil entrance connects.
Or, the described quench oil outlet of described vacuum distillation tower and the quench oil of described atmospheric distillation tower
Entrance connects, and the light fraction produced by vacuum distillation tower, as the raw material of atmospheric distillation tower, circulates fractional distillation.
Or, the circulation heavy oil outlet of described vacuum distillation tower and the weight of described floating bed hydrogenation reactor
Oil-in connects, by the heavy component circular treatment of vacuum distillation tower.
Or, the hydrogen outlet of described gas trap enters with the hydrogen of described floating bed hydrogenation reactor
Mouth connects, and the side-product that processing system produces is directly used in system, it is achieved the self-sufficiency of hydrogen, saves
Hydrogen manufacturing cost.
The processing system of pyrolysis oil gas disclosed by the invention, farther includes cleaner unit, described cleaner unit
Outlet connect described quencher pyrolysis oil gas entrance.
Or, farther including regulator, the air intake of described regulator connects the cold of described quencher
But oil gas vent, the gas outlet of described regulator connects the cooling oil gas entrance of described atmospheric distillation tower.
Wherein, the catalyst used by described floating bed hydrogenation reactor, including in iron containing compounds
Plant or several.Or, described catalyst include pyrite, red mud, bloodstone, laterite-type nickel ore,
One or more in limonite.The particle size range of described catalyst is 5～10 μm.Described catalyst contains
Amount accounts for the 0.1～5.0% of reaction raw materials gross weight；It is preferably 0.5～3.0%.
Invention additionally discloses a kind of processing method being pyrolyzed oil gas, apply above-mentioned processing system, method
Including:
Chilling: pyrolysis oil gas obtains condensing heavy oil and cooling oil gas under cooling oil spray effect；
Air-distillation: cooling oil gas distillation obtains heavy oil at the bottom of pyrolysis gas and atmospheric tower；
It is hydrocracked: heavy oil at the bottom of atmospheric tower generates hydrogenation products under the effect of catalyst and hydrogen；
Gas-liquid separation: hydrogenation products is isolated to cracked gas and cracked oil；
Decompression distillation: by cracked oil decompression distillation, obtain quench oil and VACUUM TOWER BOTTOM heavy oil, quench oil
Supply quencher；
Gas separates: with pyrolysis gas, cracked gas is carried out gas and separates, obtain hydrogen and fuel gas.
Further, it is anti-that the condensation heavy oil that described chilling step obtains is admitted to described floating bed hydrogenation
Device is answered to be hydrocracked.
Or, the VACUUM TOWER BOTTOM heavy oil of described decompression distillation gained is admitted to the reaction of described floating bed hydrogenation
Device is hydrocracked, by the heavy component circular treatment of vacuum distillation tower.
Or, the quench oil of described decompression distillation gained is admitted to described atmospheric distillation tower and carries out normal pressure steaming
Evaporating, the light components produced by vacuum distillation tower, as the raw material of atmospheric distillation tower, circulates fractional distillation.
Or, the isolated hydrogen of described gas trap is admitted in described floating bed hydrogenation reactor,
The side-product that processing system produces is directly used in system, it is achieved the self-sufficiency of hydrogen, saves hydrogen manufacturing cost.
Further, also include the step of pyrolysis oil gas dedusting before chilling step.
The step of stable cooling oil gas is also included, with stable between chilling step and air-distillation step
The just pressure of cold oil gas, protects atmospheric distillation tower.
Wherein, pyrolysis oil gas is cooled to 350～420 DEG C at quencher；It is preferably 365～400 DEG C；Enter
The cooling oil gas temperature entering atmospheric distillation tower is 345～385 DEG C.
Cracked oil is obtained through decompression distillation≤500 DEG C of light fractions are as quench oil.
What technical solution of the present invention was brought has the beneficial effects that:
(1) present invention has coupled coal tar oil recovery and the course of processing during coal fast pyrogenation, adopts
With the light fraction part cooling medium as pyrolysis oil gas that reduces pressure of floating bed hydrogenation product, part conduct
Atmospheric distillation tower feeds, this cooling medium better heat stability, it is to avoid the secondary condensation in cooling procedure
Green coke, avoids water-cooled simultaneously and produces substantial amounts of phenol-containing wastewater, can improve light oil yield.
(2) pyrolysis oil gas advanced person's row quenching, cools down the heavy tar in oil gas, relatively
The tar of lightweight and pyrolysis gas enter atmospheric distillation tower, continue separate out light ends, can be fully sharp
With first cold oil gas heat, it is to avoid redistilled energy consumption after cooling completely.
(3) the isolated hydrogen of pyrolysis gas is used for coal tar heavy ingredients suspension bed hydroprocessing cracking, it is achieved
The self-sufficiency of hydrogen, saves hydrogen manufacturing cost.
Accompanying drawing explanation
Fig. 1 is the structural representation sketch that the present invention is pyrolyzed processing system one embodiment of oil gas；
Fig. 2 is the schematic flow sheet that the present invention is pyrolyzed the processing method of oil gas.
Description of reference numerals:
1, pyrolysis oven, 2, pyrolysis oil gas, 3, cleaner unit, 5, pyrolysis oil cooler out of breath, 6, just
Cold oil gas, 7, regulator, 8, cooling oil gas 9, atmospheric distillation tower, 10, pyrolysis gas, 11, stone
Naphtha fraction, 12, diesel oil distillate, 13, heavy oil fraction at the bottom of atmospheric tower, 14, condensation heavy oil fraction,
15, catalyst, 16, floating bed hydrogenation reactor, 17, hydrogenation products, 18 gas-liquid separators, 19,
Cracked oil, 20, cracked gas, 21, gas trap, 22, hydrogen, 23, fuel gas, 24, subtract
Pressure distillation column, 27, quench oil (≤500 DEG C of fractions), 28, VACUUM TOWER BOTTOM heavy oil fraction (> 500 DEG C
Fraction).
Detailed description of the invention
The processing system of pyrolysis oil gas involved in the present invention and processing method, be particularly suited for low order
Coal tar oil recovery and lighting during coal fast pyrogenation, be also applied for coal, oil shale, oil-sand,
Bitumen, biomass, rubbish etc. obtain oil, the recovery of gas and processing by pyrolysis or dry distilling.
For fast pyrogenation oil gas contains more thermally labile component, if all condensation post-treatment needs
Will thermal distillation again, distilling apparatus is prone to the defect of coking, the present invention first by heavy tar chilling separate,
Just cold oil gas enters distillation column and isolates light ends, can make full use of the heat in pyrolysis oil gas, weight
Matter tar carries out floating bed hydrocracking process, can obtain more light Fuel.
Recovery and the processing of fast pyrogenation coal tar are coupled by the present invention, utilize heavy coal tar to hang
Part light fraction (fractions of≤500 DEG C) after floating bed hydrogenation is as the quench oil of pyrolysis oil gas, part
As the charging of atmospheric distillation tower, heavy oil at the bottom of heavy oil, part reduced pressure tower at the bottom of condensation heavy oil, atmospheric tower
The fraction that (> is 500 DEG C) as the raw material of floating bed hydrocracking, make coal tar fully be reclaimed and
Comprehensive utilization.
Fast pyrogenation oil gas obtains condensation heavy oil and first cold oil gas after chilling, and first cold oil gas is stablized laggard
Enter atmospheric distillation tower and isolate heavy oil at the bottom of naphtha cut, diesel oil distillate and tower, condensation heavy oil and tower
End heavy oil, as suspension bed material, obtains cracked gas and cracked oil, cracked oil after hydrogenated cracking reaction
Through decompression distillation acquisition decompression light fraction as quench oil, a quench oil part is as the urgency of pyrolysis oil gas
Cold medium, a part is as the charging of atmospheric distillation tower, and the VACUUM TOWER BOTTOM heavy oil containing catalyst is a part of
Getting rid of outward, a part loops back suspension bed.
The present invention discloses a kind of processing system being pyrolyzed oil gas, including: quencher, it is provided with pyrolysis oil gas
Entrance, quench oil entrance, cooling oil gas vent and condensation heavy oil outlet；Atmospheric distillation tower, is provided with cold
But oil gas entrance, pyrolysis gas outlet, quench oil entrance and heavy oil outlet；Described cooling oil gas enters
Mouth is connected with the cooling oil gas vent of described quencher；Floating bed hydrogenation reactor, be provided with heavy oil entrance,
Hydrogenation products outlet, hydrogen inlet；Described heavy oil entrance connects with the heavy oil outlet of described atmospheric distillation tower
Connect；Gas-liquid separator, is provided with hydrogenation products entrance, cracking gas exit and cracked oil outlet；Decompression is steamed
Evaporate tower, be provided with cracked oil entrance, quench oil outlet and circulation heavy oil outlet；Described cracked oil entrance with
The cracked oil outlet of described gas-liquid separator connects；The outlet of described quench oil and the chilling of described quencher
Oil-in connects；Gas trap, is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen outlet；Institute
State pyrolysis gas entrance to be connected with the pyrolysis gas outlet of described atmospheric distillation tower；Described cracked gas entrance and institute
The cracking gas exit stating gas-liquid separator connects.
Fig. 1 is the structural representation sketch of pyrolysis oil gas processing system one embodiment of the present invention, such as Fig. 1 institute
Show, the present invention be pyrolyzed the processing system of oil gas include pyrolysis of coal unit 1, pyrolysis oil gas dust removing units 3,
Pyrolysis oil gas quenching unit 5, first cold oil gas stablize unit 7, air-distillation unit 9, floating bed hydrogenation
Cracking Unit 16, gas-liquid separation unit 18, gas separation unit 21, decompression distillation unit 24.
Described pyrolysis oil gas dust removing units 3 includes cleaner unit, and pipeline connects the pyrolysis of pyrolysis of coal unit 1
Oil gas vent and the entrance of cleaner unit；The outlet of cleaner unit is connected to pyrolysis oil cold list out of breath by pipeline
The pyrolysis oil gas entrance of unit 5, will be transported to dedusting by the pyrolysis oil gas 2 discharged in pyrolysis of coal unit 1
Device enters quencher after removing large particulate matter.The setting of cleaner unit, can remove pyrolysis oil gas in big
The dust-like impurity of grain, reduces blocking and the coking of dust of follow-up equipment, reduces the use longevity of equipment
Life.
Described pyrolysis oil gas quenching unit 5 includes that quencher, quencher are provided with pyrolysis oil gas entrance, urgency
Cold oil entrance, cooling oil gas vent and condensation heavy oil outlet.Quench oil from quench oil entrance sprayed into
In quencher, the pyrolysis oil gas 4 after removing dust enters quencher, through quench oil raindrop battle array, temperature
It is lowered, becomes cooling oil gas 6, cooling oil gas vent discharge quencher.Pyrolysis oil gas is at pyrolysis gas
Quenching unit is cooled to 350～420 DEG C；It is preferably 365～400 DEG C.
First cold oil gas is stablized unit 7 and is included regulator, and the air intake of regulator connects chilling by pipeline
The quench oil outlet of device, the gas outlet of regulator connects the cooling oil gas entrance of follow-up atmospheric distillation tower,
The cooling oil gas 8 of steady air current is sent into atmospheric distillation tower.
It should be noted that the pyrolysis oil gas dust removing units described in the present embodiment and first cold oil gas are stable
Unit is not the prerequisite facility of the present invention, depending on pending pyrolysis oil gas impurities and air-flow
Degree of stability depending on, the present invention is not limited.
Air-distillation unit 9 refers to that atmospheric distillation tower, distillation column arrange bottom feed mouth, top gas
Outlet, heavy oil component outlet at the bottom of naphtha cut lateral line withdrawal function mouth, diesel oil distillate lateral line withdrawal function mouth and tower.
Bottom distillation column, charging aperture i.e. cools down oil gas entrance and quench oil entrance, by going out of pipeline and regulator
QI KOU, part quench oil pipeline 27 connect, for the material inlet of atmospheric distillation tower.Top gas goes out
Mouth is pyrolysis gas outlet, is derived by the pyrolysis gas 10 of generation.Naphtha cut lateral line withdrawal function mouth derives stone
Naphtha fraction 11.Diesel oil distillate lateral line withdrawal function mouth derives diesel oil distillate 12.Heavy oil component outlet guide at the bottom of tower
Go out heavy oil 13 at the bottom of atmospheric tower.The cooling oil gas temperature entering atmospheric distillation tower is generally 345～385 DEG C.
Floating bed hydrocracking unit 16 includes floating bed hydrogenation reactor.Floating bed hydrogenation reactor sets
There are the heavy oil entrance of bottom, the hydrogenation products outlet on top, hydrogen inlet.Heavy oil entrance steams with normal pressure
The heavy oil outlet evaporating tower connects.
The hydrogenation products 17 that floating bed hydrogenation reactor 16 produces flows to gas-liquid separation unit 18 and separates
Go out cracked gas 20 and cracked oil 19, discharged by top gas outlet and bottom liquid outlet respectively.
Floating bed hydrocracking unit operating condition is generally: reaction pressure 9～25Mpa, preferably
10～20Mpa；Reaction temperature is 380～480 DEG C, preferably 400～470 DEG C.
Gas separation unit 21 includes that gas trap, gas trap are provided with pyrolysis gas entrance, cracking
Gas entrance, hydrogen outlet.Pyrolysis gas entrance is connected with the pyrolysis gas outlet of atmospheric distillation tower；Cracked gas
Entrance is connected with the cracking gas exit of gas-liquid separator.Gas trap is by pyrolysis gas 10, cracked gas 20
Separating, isolated hydrogen 22 sends into floating bed hydrogenation reactor, and the fuel gas 23 of generation can
Use as fuel after collection.
The cracked oil 19 that gas-liquid separation unit 18 produces is admitted to decompression distillation unit 24.Decompression distillation
Unit includes that vacuum distillation tower, vacuum distillation tower are provided with cracked oil entrance, quench oil outlet and circulation weight
Oil export；Cracked oil entrance exports with the cracked oil of gas-liquid separator and is connected；Quench oil outlet and chilling
The quench oil entrance of device connects.
Vacuum distillation tower is provided with cracked oil entrance, quench oil outlet and circulation heavy oil outlet；Cracked oil enters
Mouth exports with the cracked oil of gas-liquid separator and is connected；The quench oil 27 that vacuum distillation tower generates is by quench oil
Outlet and the quench oil entrance of quencher, and the bottom feed mouth connection of atmospheric distillation tower；Circulation weight
The VACUUM TOWER BOTTOM heavy oil 28 of generation is sent into floating bed hydrogenation reactor by oil export so that quencher cold
At the bottom of dignified oily 14, atmospheric tower, heavy oil 13 and VACUUM TOWER BOTTOM heavy oil 28 become floating bed hydrogenation reactor
Raw material.Using cracked oil through decompression distillation gained≤fraction of 500 DEG C is as quench oil.This area skill
Art personnel according to GB/T 9168-1997, can control the parameter of vacuum distillation tower, obtains the upper of cracked oil
State cut point, thus control the composition of quench oil.
Floating bed hydrogenation reactor in the processing system of this pyrolysis oil gas, catalyst 15 used is solid
Body beaded catalyst, solid particle catalyst selects one or more in iron containing compounds, such as ferrum
Oxide, the sulfate of ferrum, the sulfide of ferrum, ferrum muriatic one or more；Can also be
The form of mineral dust, such as in pyrite, red mud, bloodstone, laterite-type nickel ore, limonite
Planting or several, catalyst particle size scope is 5～10 μm, and addition accounts for reaction raw materials gross weight
0.1～5.0%, preferably 0.5～3.0%.
Apply above-mentioned processing system, invention additionally discloses a kind of processing method being pyrolyzed oil gas, be used for
Reclaiming and processing pyrolysis oil gas, processing method specifically includes following steps:
Chilling: pyrolysis oil gas obtains condensing heavy oil and cooling oil gas under cooling oil spray effect；
Air-distillation: cooling oil gas distillation obtains heavy oil at the bottom of pyrolysis gas and atmospheric tower；
It is hydrocracked: heavy oil at the bottom of atmospheric tower generates hydrogenation products under the effect of catalyst and hydrogen；
Gas-liquid separation: hydrogenation products is isolated to cracked gas and cracked oil；
Decompression distillation: by cracked oil decompression distillation, obtain quench oil and VACUUM TOWER BOTTOM heavy oil, quench oil
Supply quencher；
Gas separates: with pyrolysis gas, cracked gas is carried out gas and separates, obtain hydrogen and fuel gas.
In order to remove the large granular impurity in pyrolysis gas, also include removing pyrolysis oil gas before chilling step
The step of dirt；In order to protect air-distillation equipment, before air-distillation step, also include stable cooling
The step of oil gas.
In order to save the energy, the side-product that cyclic utilization system of the present invention produces, such as:
Condensation heavy oil chilling step obtained is admitted to floating bed hydrogenation reactor and is hydrocracked；
Or, the VACUUM TOWER BOTTOM heavy oil of decompression distillation gained is admitted to floating bed hydrogenation reactor hydrogenation
Cracking；
Or, the quench oil of decompression distillation gained is admitted to atmospheric distillation tower and carries out air-distillation；
Or, isolated for gas trap hydrogen is admitted in floating bed hydrogenation reactor.
Specifically, as in figure 2 it is shown, the processing method that the present invention is pyrolyzed oil gas includes:
(1) entering cleaner unit from pyrolysis oven pyrolysis oil gas out, the mechanical admixture such as removing dust is laggard
Enter pyrolysis oil gas quenching unit, quenching unit is pyrolyzed oil gas by the part chilling from decompression distillation
Oil Quench, it is thus achieved that condensation heavy oil and first cold oil gas；
(2) just cold oil gas enter behind regulator atmospheric distillation tower isolate pyrolysis gas, naphtha cut,
Heavy oil at the bottom of diesel oil distillate, tower；
(3) the condensation heavy oil of heavy oil at the bottom of tower and quenching unit mixes as floating bed hydrocracking unit
Raw material, under the effect of catalyst and hydrogen, coal tar heavies is through slurry-bed hydrocracking
Rear entrance gas-liquid separation unit, isolates cracked gas and cracked oil；
(4) cracked oil enters vacuum distillation tower and isolates overhead light-end (≤500 DEG C of fractions) and tower
500 DEG C of end heavy oil (> fraction), light fraction, as quench oil, is partly into pyrolysis gas quenching unit,
A part is as the raw material of atmospheric distillation tower, and heavy oil partial at the bottom of tower loops back floating bed hydrocracking unit,
Part is outer gets rid of；
(5) cracked gas and pyrolysis gas enter gas separation unit, and isolated hydrogen adds as suspension bed
The hydrogen source of hydrogen Cracking Unit, other gas is as fuel gas.
The present invention is pyrolyzed the processing method of oil gas, and fast pyrogenation oil gas enters after the coldest air-distillation
Tower, isolates pyrolysis gas component, naphtha cut, diesel oil distillate and normal pressure heavy component, normal pressure
Heavy component carries out slurry-bed hydrocracking, and after gas-liquid separation, liquid phase enters vacuum distillation tower,
Isolating light fraction and heavy distillat, a light fraction part cools down the oil from pyrolysis oven as quench oil
Gas, a part feeds as atmospheric tower, and heavy distillat part loops back floating bed hydrogenation reactor, cracking
Gas and pyrolysis gas enter gas trap, isolate hydrogen and other gas, and hydrogen adds as suspension bed
The hydrogen source of hydrogen, other gas is as fuel gas.
Describe the present invention in detail by embodiment below, but embodiment is not thereby limiting the invention
Range.Detailed description of the invention, according to technological process shown in Fig. 1, reclaims and processes Hunchun low order
The middle coalite tar that coal fast pyrogenation produces.
The present invention uses Huichun Station of Jilin Province low-order coal as pyrolysis feed coal, and its main property character is shown in Table 1.
Table 1 Hunchun low-order coal main character
Embodiment 1
Oil gas from pyrolysis oven is cooled to 380 DEG C at pyrolysis gas quenching unit, after regulator is stable
With 375 DEG C of entrance atmospheric distillation towers, pyrolysis gas is isolated at top, and side line isolates naphtha cut, bavin
Oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil and VACUUM TOWER BOTTOM heavy oil are as floating bed hydrocracking list
The charging of unit, slurry-bed hydrocracking temperature 420 DEG C, pressure 12Mpa, catalyst is Lateritic Soil
Nickel minerals powder particle, particle diameter is 5～10 μm, addition 2.0%, and reaction primary product distribution is shown in Table 2.
From table 2, green coke amount only has 0.5%, light oil (naphtha cut and diesel oil distillate summation) yield
It is 88.3%.
Embodiment 2
Oil gas from pyrolysis oven is cooled to 400 DEG C at pyrolysis gas quenching unit, after regulator is stable
With 385 DEG C of entrance atmospheric distillation towers, pyrolysis gas is isolated at top, and side line isolates naphtha cut, bavin
Oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil and VACUUM TOWER BOTTOM heavy oil are as floating bed hydrocracking list
The charging of unit, slurry-bed hydrocracking temperature 480 DEG C, pressure 25Mpa, catalyst is red mud powder
End granule, particle diameter is 10 μm, addition 3.0%, and reaction primary product distribution is shown in Table 2.Can by table 2
Seeing, green coke amount is 0.8%, and light oil yield is 89.3%.
Embodiment 3
Oil gas from pyrolysis oven is cooled to 365 DEG C at pyrolysis gas quenching unit, after regulator is stable
With 360 DEG C of entrance atmospheric distillation towers, pyrolysis gas is isolated at top, and side line isolates naphtha cut, bavin
Oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil and VACUUM TOWER BOTTOM heavy oil are as floating bed hydrocracking list
The charging of unit, slurry-bed hydrocracking temperature 470 DEG C, pressure 20Mpa, catalyst is Lateritic Soil
Nickel minerals and red mud powder particle (respectively account for 50%, mass fraction, lower with), particle diameter is 7 μm, addition
0.5%, reaction primary product distribution is shown in Table 2.From table 2, green coke amount is 0.85%, light oil yield
It is 88.1%.
Embodiment 4
Oil gas from pyrolysis oven is cooled to 350 DEG C at pyrolysis gas quenching unit, after regulator is stable
With 345 DEG C of entrance atmospheric distillation towers, pyrolysis gas is isolated at top, and side line isolates naphtha cut, bavin
Oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil and VACUUM TOWER BOTTOM heavy oil are as floating bed hydrocracking list
The charging of unit, slurry-bed hydrocracking temperature 380 DEG C, pressure 10Mpa, catalyst is limonite
Powder particle, particle diameter is 10 μm, addition 5%, and reaction primary product distribution is shown in Table 2.By table 2
Visible, green coke amount is 0.75%, and light oil yield is 86.0%.
Embodiment 5
Oil gas from pyrolysis oven is cooled to 420 DEG C at pyrolysis gas quenching unit, after regulator is stable
With 385 DEG C of entrance atmospheric distillation towers, pyrolysis gas is isolated at top, and side line isolates naphtha cut, bavin
Oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil and VACUUM TOWER BOTTOM heavy oil are as floating bed hydrocracking list
The charging of unit, slurry-bed hydrocracking temperature 400 DEG C, pressure 9Mpa, catalyst is laterite nickel
And pyrite (70%) powder particle (30%), particle diameter is 8 μm, addition 0.1%, and reaction is main
Products distribution is wanted to be shown in Table 2.From table 2, green coke amount is 0.68%, and light oil yield is 88.0%.
Comparative example 1
Pyrolysis oil gas from pyrolysis oven directly enters atmospheric distillation tower after regulator is stable, and tower top divides
Separating out pyrolysis gas, heavy oil at the bottom of naphtha cut, diesel oil distillate and tower isolated by side line, arranges at the bottom of tower
Tower top heavy oil refluxes,
Heavy oil backflow is shown in Table 2 as the cooling medium of pyrolysis oil gas, reaction primary product distribution.By table 2
Visible, in this comparative example, green coke amount is 17.3%, and mainly at air-distillation tower bottom green coke, light oil is received
Rate also only has 68.3%.Highlight the present invention to be pyrolyzed oil gas and first after just cooling down, enter back into atmospheric distillation tower
Advantage.
Comparative example 2
Pyrolysis oil gas from pyrolysis oven use conventional coking process coal-tar middle oil and coal gas cool back debit
As the raw material of floating bed hydrocracking unit after method, i.e. tar are completely cooled, floating bed hydrogenation is anti-
Answering operating condition same as in Example 1, floating bed hydrogenation product enters vacuum distillation tower, separates
The light components gone out enters air-distillation unit, and heavy component loops back floating bed hydrogenation reactor, instead
Primary product distribution is answered to be shown in Table 2.
From table 2, after the coal-tar middle oil cooling completely of this comparative example, it is re-used as floating bed hydrocracking raw material,
The increase of energy consumption is apparent from, the most compared with Example 1, and naphtha cut and diesel oil distillate
Yield be significantly reduced, light oil yield reduce by 12.4 percentage points.
Table 2 embodiment and the distribution of comparative example primary product
What present disclosure was touched upon is exemplary embodiment, is defining without departing from claims
Protection domain in the case of, each embodiment of the application can be made various changes and modifications.
Therefore, it is all that described embodiment is intended in the protection domain of appended claims
This type of changes, revises and deform.Additionally, unless the context outside indication, occur in the singular
Word includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment complete
Portion or a part can be in conjunction with all or part of uses of any other embodiments.
Claims (10)
1. the processing system being pyrolyzed oil gas, it is characterised in that including:
Quencher, is provided with pyrolysis oil gas entrance, quench oil entrance, cooling oil gas vent and condensation heavy oil
Outlet；
Atmospheric distillation tower, is provided with cooling oil gas entrance, pyrolysis gas outlet, quench oil entrance, Yi Jichong
Oil export；Described cooling oil gas entrance is connected with the cooling oil gas vent of described quencher；
Floating bed hydrogenation reactor, is provided with heavy oil entrance, hydrogenation products outlet, hydrogen inlet；Described
Heavy oil entrance exports with the heavy oil of described atmospheric distillation tower and is connected；
Gas-liquid separator, is provided with hydrogenation products entrance, cracking gas exit and cracked oil outlet；Described add
Hydrogen product inlet exports with the hydrogenation products of described floating bed hydrogenation reactor and is connected；
Vacuum distillation tower, is provided with cracked oil entrance, quench oil outlet and circulation heavy oil outlet；Described split
Carburetion entrance exports with the cracked oil of described gas-liquid separator and is connected；The outlet of described quench oil and described urgency
The quench oil entrance of cooler connects；
Gas trap, is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen outlet；Described pyrolysis gas
Entrance is connected with the pyrolysis gas outlet of described atmospheric distillation tower；Described cracked gas entrance divides with described gas-liquid
Cracking gas exit from device connects.
2. the processing system being pyrolyzed oil gas as claimed in claim 1, it is characterised in that described chilling
The condensation heavy oil outlet of device is connected with the heavy oil entrance of described floating bed hydrogenation reactor；
Or, the described quench oil outlet of described vacuum distillation tower and the quench oil of described atmospheric distillation tower
Entrance connects；
Or, the circulation heavy oil outlet of described vacuum distillation tower and the weight of described floating bed hydrogenation reactor
Oil-in connects；
Or, the hydrogen outlet of described gas trap enters with the hydrogen of described floating bed hydrogenation reactor
Mouth connects.
3. the processing system being pyrolyzed oil gas as claimed in claim 1, it is characterised in that wrap further
Including cleaner unit, the outlet of described cleaner unit connects the pyrolysis oil gas entrance of described quencher；
Or, farther including regulator, the air intake of described regulator connects the cold of described quencher
But oil gas vent, the gas outlet of described regulator connects the cooling oil gas entrance of described atmospheric distillation tower.
4. the processing system being pyrolyzed oil gas as claimed in claim 1, it is characterised in that described suspension
Catalyst used by bed hydroprocessing reactor, including one or more in iron containing compounds；
Or, described catalyst includes pyrite, red mud, bloodstone, laterite-type nickel ore, limonite
In one or more；
The particle size range of described catalyst is 5～10 μm；
Described catalyst content accounts for the 0.1～5.0% of reaction raw materials gross weight；It is preferably 0.5～3.0%.
5. it is pyrolyzed a processing method for oil gas, applies the system as claimed in claim 1, its feature
It is, including:
Chilling: pyrolysis oil gas obtains condensing heavy oil and cooling oil gas under cooling oil spray effect；
Air-distillation: cooling oil gas distillation obtains heavy oil at the bottom of pyrolysis gas and atmospheric tower；
It is hydrocracked: heavy oil at the bottom of atmospheric tower generates hydrogenation products under the effect of catalyst and hydrogen；
Gas-liquid separation: hydrogenation products is isolated to cracked gas and cracked oil；
Decompression distillation: by cracked oil decompression distillation, obtain quench oil and VACUUM TOWER BOTTOM heavy oil, quench oil
Supply quencher；
Gas separates: with pyrolysis gas, cracked gas is carried out gas and separates, obtain hydrogen and fuel gas.
6. processing method as claimed in claim 5, it is characterised in that described chilling step obtains
Condensation heavy oil is admitted to described floating bed hydrogenation reactor and is hydrocracked；
Or, the VACUUM TOWER BOTTOM heavy oil of described decompression distillation gained is admitted to the reaction of described floating bed hydrogenation
Device is hydrocracked；
Or, the quench oil of described decompression distillation gained is admitted to described atmospheric distillation tower and carries out normal pressure steaming
Evaporate；
Or, the isolated hydrogen of described gas trap is admitted in described floating bed hydrogenation reactor.
7. processing method as claimed in claim 5, it is characterised in that also include before chilling step
Step by pyrolysis oil gas dedusting.
8. processing method as claimed in claim 5, it is characterised in that steam in chilling step and normal pressure
Evaporate the step also including stable cooling oil gas between step.
9. processing method as claimed in claim 5, it is characterised in that pyrolysis oil gas is at quencher quilt
It is cooled to 350～420 DEG C；It is preferably 365～400 DEG C；The cooling oil gas temperature entering atmospheric distillation tower is
345～385 DEG C.
10. processing method as claimed in claim 5, it is characterised in that described quench oil is cracking
Oil obtain through decompression distillation≤light fraction of 500 DEG C.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108611104A (en) * | 2018-06-19 | 2018-10-02 | 天津大学 | A kind of method and apparatus that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating |
| CN112831344A (en) * | 2019-11-22 | 2021-05-25 | 中国石化工程建设有限公司 | Separation method and separation system for hydrocracking reaction products in slurry bed |
| US11534746B2 (en) | 2018-04-06 | 2022-12-27 | Utah State University | Red mud compositions and methods related thereto |
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| CN1295112A (en) * | 2000-11-02 | 2001-05-16 | 中国石油天然气股份有限公司 | Normal pressure suspension bed hydrogenation process adopting liquid multiple-metal catalyst |
| CN102443406A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil distillation method |
| CN206051957U (en) * | 2016-07-01 | 2017-03-29 | 北京神雾环境能源科技集团股份有限公司 | A kind of processing system of pyrolysis oil gas |
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| CN1295112A (en) * | 2000-11-02 | 2001-05-16 | 中国石油天然气股份有限公司 | Normal pressure suspension bed hydrogenation process adopting liquid multiple-metal catalyst |
| CN102443406A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil distillation method |
| CN206051957U (en) * | 2016-07-01 | 2017-03-29 | 北京神雾环境能源科技集团股份有限公司 | A kind of processing system of pyrolysis oil gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US11534746B2 (en) | 2018-04-06 | 2022-12-27 | Utah State University | Red mud compositions and methods related thereto |
| US11938470B2 (en) | 2018-04-06 | 2024-03-26 | Utah State University | Red mud compositions and methods related thereto |
| CN108611104A (en) * | 2018-06-19 | 2018-10-02 | 天津大学 | A kind of method and apparatus that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating |
| CN112831344A (en) * | 2019-11-22 | 2021-05-25 | 中国石化工程建设有限公司 | Separation method and separation system for hydrocracking reaction products in slurry bed |
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