CN206051957U - A kind of processing system of pyrolysis oil gas - Google Patents
A kind of processing system of pyrolysis oil gas Download PDFInfo
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- CN206051957U CN206051957U CN201620683944.8U CN201620683944U CN206051957U CN 206051957 U CN206051957 U CN 206051957U CN 201620683944 U CN201620683944 U CN 201620683944U CN 206051957 U CN206051957 U CN 206051957U
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Abstract
This utility model discloses a kind of processing system of pyrolysis oil gas.The system includes：Gas trap and the quencher being sequentially connected, atmospheric distillation tower, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower；The cooling oil gas vent of quencher connects the cooling oil gas entrance of atmospheric distillation tower, and chilling oil-in connects the chilling oil export of vacuum distillation tower；The heavy oil entrance of the heavy oil outlet connection floating bed hydrogenation reactor of atmospheric distillation tower, pyrolysis gas outlet connect the pyrolysis gas entrance of gas trap；The hydrogenation products inlet port of floating bed hydrogenation reactor connects the hydrogenation products entrance of gas-liquid separator；The cracking oil export of gas-liquid separator connects the cracking oil-in of vacuum distillation tower, and cracking gas exit connects the cracked gas entrance of gas trap.Pyrolysis oil gas is first carried out just cold by this utility model with the decompression light fraction part of floating bed hydrogenation product as the cooling medium of pyrolysis oil gas, it is to avoid the secondary condensation green coke in cooling procedure, improves light oil yield.
Description
Technical field
This utility model is related to a kind of system by pyrolysis oil gas processing light-weight fuel oil.In particular, be
During coal fast pyrogenation, coupling is pyrolyzed the recovery of oil gas and the course of processing, the system for obtaining light-weight fuel oil.
Background technology
Coal sub-prime is using the effective way for being considered as Coal Clean efficient utilization, and China " 13 " Coal Chemical Industry
The direction given priority to.It is exactly to separate the heterogeneity in coal by pyrolysises that the sub-prime of coal is utilized, including
Coal gas, tar and semicoke for finally giving etc..Wherein, tar can produce gasoline, diesel oil by hydrogenation, and semicoke is by pyrolysis
Become the clean fuel of low volatile, low-sulfur, replace dissipating the pollution for coal reduction being burnt to air.
" tap " that coal sub-prime is utilized is the pyrolytic technique of coal, and pyrolytic technique to be extracted the tar of scale production quantities, coal gas.
With the progress of science and technology, using scale, maximization, single set pyrolysis of coal unit scale is also more and more large-scale therewith for coal sub-prime,
And pyrolysis rate is also improved rapidly, the time of staying of the coal in pyrolysis oven is only several seconds, and pyrolysis oil gas overflows speed soon, and produces
The coal tar for going out mostly is middle coalite tar, and its property has bigger difference with the coal tar of conventional coking output.
In existing process of coking, coke-stove gas is 650～750 DEG C from carbonizing chamber tedge effusion temperature, first in bridge
70～75 DEG C of ammonia is sprayed in pipe and discharge, coal gas is cooled to 80～85 DEG C, and 60% tar is cooled in coal gas, condensation
What is got off is heavy tar, and sprinkling ammonia ensures tar mobility.Using this conventional processing mode come treatment scale
The pyrolysis oil gas that coal fast pyrogenation is produced, can consume substantial amounts of ammonia, and produce large amount of sewage；Although its light component content is higher than
High temperature coal-tar, but contain in fast pyrogenation coal tar more toluene insolubles, mainly coal dust and coal ash, and viscosity compared with
Greatly, emulsifying degree is high, heat stability is poor, difficulty of processing is big, and comprehensive profit is realized in the recovery and processing scheme for needing appropriate design
With to increase economic efficiency.
A kind of existing raw coke oven gas cooling fractional method and coking technology, are that the raw coke oven gas that will be discharged from coke furnace carbonization chamber is dividing
Cooled down in distillation unit step by step, propose the different fractions in raw coke oven gas, fractional distillation dress according to fraction boiling point order from high to low step by step
Put, and subsequent recovery raw coke oven gas.This mode,
650～700 DEG C of raw coke oven gas is directly entered into fractionating device, Colophonium, segregation apparatuss bottom is fractionated out first in fractionating device bottom
Portion's temperature is higher, the easy coking of asphalt component.Every grade of dephlegmator arranges dividing plate and only can cause point in middle setting projection through hole
Precision reduction is evaporated, the heavy constituent of non-total condensation can be brought in light component in raw coke oven gas.In addition arrange in every level shunt device
Spray thrower, reflux pump and temperature-adjusting device, technique are complex, and the long period stable operation of device is relatively difficult to ensure card, therefore, the party
Method is pyrolyzed the recovery of oil gas in being unsuitable for the coal fast pyrolysis process of scale.
Separately there are the slurry bed system and fixed bed coupling process of a kind of full fraction of coal tar hydrogenation, the method is will be pretreated
Coal tar carries out fractional distillation Jing after slurry bed system is hydrocracked, and light components obtained by fractional distillation enter fixed bed hydrogenation refined unit, middle
Fraction and catalyst loop back slurry bed system hydrogenation reactor, and heavy component returns burnt after partial catalyst and coke is removed by filtration
Oily pretreatment unit circulation hydrogenation.The method is that for containing, light components are more by the process of full fraction of coal tar elder generation Jing slurry bed systems
Middle coalite tar, in slurry bed system hydrocracking process, gas phase hydrocarbon is more, and system pressure can be caused to raise, hydrogen dividing potential drop drop
It is low, the conversion ratio of heavy component is affected, causes to waste.
Utility model content
This utility model improves heavy group to adapt to the requirement of recovery and processing that oil gas is pyrolyzed in fast pyrolysis process
Divide conversion ratio, it is to avoid coking, propose a kind of processing system of pyrolysis oil gas.
This utility model is to be achieved through the following technical solutions foregoing invention purpose：
A kind of processing system of pyrolysis oil gas, including：Quencher, is provided with pyrolysis oil gas entrance, chilling oil-in, cooling oil
Gas exports and condenses heavy oil outlet；Atmospheric distillation tower, is provided with cooling oil gas entrance, pyrolysis gas outlet, chilling oil-in, Yi Jichong
Oil export；The cooling oil gas entrance is connected with the cooling oil gas vent of the quencher；Floating bed hydrogenation reactor, is provided with weight
Oil-in, hydrogenation products outlet, hydrogen inlet；The heavy oil entrance is connected with the heavy oil outlet of the atmospheric distillation tower；Gas-liquid
Separator, is provided with hydrogenation products entrance, cracking gas exit and cracking oil export；The hydrogenation products entrance is added with the suspension bed
The hydrogenation products outlet connection of hydrogen reactor；Vacuum distillation tower, is provided with cracking oil-in, chilling oil export and circulation heavy oil and goes out
Mouthful；The cracking oil-in is connected with the cracking oil export of the gas-liquid separator；The chilling oil export and the quencher
Chilling oil-in connection；Gas trap, is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen outlet；The pyrolysis gas entrance
It is connected with the pyrolysis gas outlet of the atmospheric distillation tower；The cracked gas entrance is connected with the cracking gas exit of the gas-liquid separator
Connect.
Further, the condensation heavy oil outlet of the quencher is connected with the heavy oil entrance of the floating bed hydrogenation reactor
Connect.
Or, the chilling oil export of the vacuum distillation tower is connected with the chilling oil-in of the atmospheric distillation tower,
Raw material of the light fraction that vacuum distillation tower is produced as atmospheric distillation tower, circulates fractional distillation.
Or, the outlet of circulation heavy oil and the heavy oil entrance of the floating bed hydrogenation reactor of the vacuum distillation tower connect
Connect, by the heavy component circular treatment of vacuum distillation tower.
Or, the hydrogen outlet of the gas trap is connected with the hydrogen inlet of the floating bed hydrogenation reactor, will
The side-product that processing system is produced is directly used in system, realizes the self-sufficiency of hydrogen, saves hydrogen manufacturing cost.
The processing system of the disclosed pyrolysis oil gas of this utility model, further includes cleaner unit, the outlet of the cleaner unit
Connect the pyrolysis oil gas entrance of the quencher.
Or, regulator is further included, the air intake of the regulator connects the cooling oil gas vent of the quencher,
The gas outlet of the regulator connects the cooling oil gas entrance of the atmospheric distillation tower.
Wherein, the catalyst used by the floating bed hydrogenation reactor, including one or more in iron containing compoundses.Or
Person, the catalyst include one or more in pyrite, red mud, bloodstone, laterite-type nickel ore, limonite.The catalysis
The particle size range of agent is 5～10 μm.The catalyst content accounts for the 0.1～5.0% of reaction raw materials gross weight；Preferably 0.5～
3.0%.
Wherein, be pyrolyzed oil gas 350～420 DEG C are cooled in quencher；Preferably 365～400 DEG C；Into air-distillation
The cooling oil temperature degree of tower is 345～385 DEG C.
Cracked oil Jing vacuum distillations are obtained≤500 DEG C of light fractions are used as quench oil.
The beneficial effect that technical solutions of the utility model are brought is：
(1) this utility model has coupled coal tar oil recovery and the course of processing during coal fast pyrogenation, using suspension
The decompression light fraction part of bed hydroprocessing product is partly fed as atmospheric distillation tower as the cooling medium of pyrolysis oil gas, and this is cold
But medium better heat stability, it is to avoid the secondary condensation green coke in cooling procedure, at the same avoid water-cooled produce it is substantial amounts of containing phenol
Sewage, can improve light oil yield.
(2) be pyrolyzed the advanced row quenching of oil gas, the heavy tar in oil gas cooled down, the tar of relative lightweight and
Pyrolysis gas enter atmospheric distillation tower, continue separate out light ends, can make full use of just cold oil gas heat, it is to avoid complete cold
But redistilled energy consumption after.
(3) hydrogen that pyrolysis gas are isolated is used for coal tar heavy ingredients suspension bed hydroprocessing cracking, realizes the self-sufficiency of hydrogen,
Save hydrogen manufacturing cost.
Description of the drawings
Fig. 1 is the structure schematic diagram that the processing system of this utility model pyrolysis oil gas unifies embodiment；
Fig. 2 is the schematic flow sheet of the processing method that this utility model is pyrolyzed oil gas.
Description of reference numerals：
1st, pyrolysis oven, 2, pyrolysis oil gas, 3, cleaner unit, 5, pyrolysis oil cooler out of breath, 6, first cold oil gas, 7, regulator, 8,
Cooling oil gas 9, atmospheric distillation tower, 10, pyrolysis gas, 11, naphtha cut, 12, diesel oil distillate, 13, atmospheric tower bottom heavy oil fraction,
14th, condense heavy oil fraction, 15, catalyst, 16, floating bed hydrogenation reactor, 17, hydrogenation products, 18 gas-liquid separators, 19, split
Carburetion, 20, cracked gas, 21, gas trap, 22, hydrogen, 23, fuel gas, 24, vacuum distillation tower, 27, quench oil (≤500
DEG C fraction), 28, VACUUM TOWER BOTTOM heavy oil fraction (>500 DEG C of fractions).
Specific embodiment
The processing system of pyrolysis oil gas involved in this utility model, during being particularly suited for low-order coal fast pyrogenation
Coal tar oil recovery and lighting, are also applied for coal, oil shale, oil-sand, bitumen, biomass, rubbish etc. by pyrolysis
Or dry distilling and obtain oil, the recovery of gas and processing.
For containing more thermally labile component in fast pyrogenation oil gas, if processing needs reheating to steam after all condensing
Evaporate, distilling apparatus are easy to the defect of coking, heavy tar chilling is first separated by this utility model, and just cold oil gas is into distillation column point
Light ends are separated out, the heat in pyrolysis oil gas, heavy tar can be made full use of to carry out floating bed hydrocracking process, can obtain
More light Fuel.
The recovery of fast pyrogenation coal tar and processing are coupled by this utility model, are added using heavy is coal tar suspension bed
Quench oil of the part light fraction (≤500 DEG C of fractions) after hydrogen as pyrolysis oil gas, partly as the charging of atmospheric distillation tower,
Condensation heavy oil, normal pressure bottom of tower heavy oil, part reduced pressure bottom of tower heavy oil (>500 DEG C of fraction) as the raw material of floating bed hydrocracking,
Coal tar is made fully to be reclaimed and be comprehensively utilized.
Fast pyrogenation oil gas obtains condensation heavy oil and first cold oil gas Jing after chilling, and air-distillation is entered after just cold oil gas is stable
Tower isolates naphtha cut, diesel oil distillate and bottom of tower heavy oil, and, used as suspension bed material, Jing adds for condensation heavy oil and bottom of tower heavy oil
Cracked gas and cracked oil are obtained after hydrogen cracking reaction, cracked oil Jing vacuum distillations obtain decompression light fraction as quench oil, chilling
Quenching medium of the oily part as pyrolysis oil gas, charging of the part as atmospheric distillation tower, VACUUM TOWER BOTTOM contain catalyst
A heavy oil part is outer to get rid of, and a part loops back suspension bed.
This utility model discloses a kind of processing system of pyrolysis oil gas, including：Quencher, is provided with pyrolysis oil gas entrance, urgency
Cold oil entrance, cooling oil gas vent and condensation heavy oil outlet；Atmospheric distillation tower, is provided with cooling oil gas entrance, pyrolysis gas outlet, urgency
Cold oil entrance and heavy oil outlet；The cooling oil gas entrance is connected with the cooling oil gas vent of the quencher；Suspension bed adds
Hydrogen reactor, is provided with heavy oil entrance, hydrogenation products outlet, hydrogen inlet；The weight of the heavy oil entrance and the atmospheric distillation tower
Oil export connects；Gas-liquid separator, is provided with hydrogenation products entrance, cracking gas exit and cracking oil export；Vacuum distillation tower, is provided with
Cracking oil-in, chilling oil export and circulation heavy oil outlet；The cracking oil-in is gone out with the cracked oil of the gas-liquid separator
Mouth connection；The chilling oil export is connected with the chilling oil-in of the quencher；Gas trap, be provided with pyrolysis gas entrance,
Cracked gas entrance, hydrogen outlet；The pyrolysis gas entrance is connected with the pyrolysis gas outlet of the atmospheric distillation tower；The cracked gas
Entrance is connected with the cracking gas exit of the gas-liquid separator.
Structure schematic diagrams of the Fig. 1 for one embodiment of this utility model pyrolysis oil gas processing system, as shown in figure 1, this reality
With the processing system of novel pyrolytic oil gas include pyrolysis of coal unit 1, pyrolysis oil gas dust removing units 3, pyrolysis oil gas quenching unit 5,
Just the stable unit 7 of cold oil gas, air-distillation unit 9, floating bed hydrocracking unit 16, gas-liquid separation unit 18, gas are separated
Unit 21, vacuum distillation unit 24.
The pyrolysis oil gas dust removing units 3 include cleaner unit, and pipeline connects the pyrolysis oil gas vent of pyrolysis of coal unit 1 and removes
The entrance of dirt device；The outlet of cleaner unit is connected to the pyrolysis oil gas entrance of pyrolysis oil gas quenching unit 5 by pipeline, will be by coal heat
The pyrolysis oil gas 2 discharged in solution unit 1 is transported to after cleaner unit removes large particulate matter and enters quencher.The setting of cleaner unit,
Oarse-grained dust-like impurity in pyrolysis oil gas can be removed, is reduced the blocking of follow-up equipment and the coking of dust, is reduced equipment
Service life.
The pyrolysis oil gas quenching unit 5 includes quencher, and quencher is provided with pyrolysis oil gas entrance, chilling oil-in, cold
But oil gas vent and condensation heavy oil outlet.Quench oil is sprayed in quencher from chilling oil-in, the pyrolysis oil after removing dust
Gas 4 enters quencher, and through quench oil raindrop battle array, temperature is lowered, and becomes cooling oil gas 6, is discharged by cooling oil gas vent anxious
Cooler.Pyrolysis oil gas is cooled to 350～420 DEG C in pyrolysis gas quenching unit；Preferably 365～400 DEG C.
Just the stable unit 7 of cold oil gas includes regulator, and the air intake of regulator connects the quench oil of quencher by pipeline
Outlet, the gas outlet of regulator connect the cooling oil gas entrance of follow-up atmospheric distillation tower, and the cooling oil gas 8 of steady air current is sent into
Atmospheric distillation tower.
It should be noted that the stable unit of pyrolysis oil gas dust removing units and first cold oil gas described in the present embodiment is not this
The prerequisite facility of utility model, depending on the degree of stability of pending pyrolysis oil gas impurities and air-flow, this reality
It is not limited with new.
Air-distillation unit 9 refers to atmospheric distillation tower, and distillation column arranges bottom feed mouth, top gas outlet, Petroleum
The outlet of fraction lateral line withdrawal function mouth, diesel oil distillate lateral line withdrawal function mouth and bottom of tower heavy oil component.Distillation column bottom charging aperture is cooling oil
Gas entrance and chilling oil-in, are connected by the gas outlet of pipeline and regulator, part chilling oil-piping 27, are atmospheric distillation tower
Material inlet.Top gas outlet is pyrolysis gas outlet, and the pyrolysis gas 10 of generation are derived.Naphtha cut lateral line withdrawal function
Mouth derives naphtha cut 11.Diesel oil distillate lateral line withdrawal function mouth derives diesel oil distillate 12.Normal pressure is derived in the outlet of bottom of tower heavy oil component
Bottom of tower heavy oil 13.Into generally 345～385 DEG C of the cooling oil temperature degree of atmospheric distillation tower.
Floating bed hydrocracking unit 16 includes floating bed hydrogenation reactor.Floating bed hydrogenation reactor is provided with the weight of bottom
Oil-in, the hydrogenation products outlet on top, hydrogen inlet.Heavy oil entrance is connected with the heavy oil outlet of atmospheric distillation tower.
The hydrogenation products 17 that floating bed hydrogenation reactor 16 is produced are conveyed to gas-liquid separation unit 18 and isolate cracked gas 20
With cracked oil 19, discharged by top gas outlet and bottom liquid outlet respectively.
Floating bed hydrocracking unit operating condition is generally：9～25Mpa of reaction pressure, preferably 10～20Mpa；Reaction
Temperature is 380～480 DEG C, preferably 400～470 DEG C.
Gas separation unit 21 includes gas trap, and gas trap is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen
Outlet.Pyrolysis gas entrance is connected with the pyrolysis gas outlet of atmospheric distillation tower；Cracked gas entrance is gone out with the cracked gas of gas-liquid separator
Mouth connection.Pyrolysis gas 10, cracked gas 20 are separated by gas trap, and the hydrogen 22 isolated sends into floating bed hydrogenation reaction
Device, the fuel gas 23 of generation can be used as fuel after collecting.
The cracked oil 19 that gas-liquid separation unit 18 is produced is admitted to vacuum distillation unit 24.Vacuum distillation unit includes decompression
Distillation column, vacuum distillation tower are provided with cracking oil-in, chilling oil export and circulation heavy oil outlet；Cracking oil-in and gas-liquid separation
The cracking oil export connection of device；Chilling oil export is connected with the chilling oil-in of quencher.
Vacuum distillation tower is provided with cracking oil-in, chilling oil export and circulation heavy oil outlet；Cracking oil-in and gas-liquid point
Cracking oil export from device connects；Quench oil of the quench oil 27 that vacuum distillation tower is generated by chilling oil export with quencher enters
Mouthful, and the bottom feed mouth connection of atmospheric distillation tower；The VACUUM TOWER BOTTOM heavy oil 28 of generation is sent into suspension by circulation heavy oil outlet
Bed hydroprocessing reactor so that the condensation heavy oil 14 of quencher, normal pressure bottom of tower heavy oil 13 and VACUUM TOWER BOTTOM heavy oil 28 become suspension
The raw material of bed hydroprocessing reactor.Using obtained by cracked oil Jing vacuum distillations≤500 DEG C of fraction is used as quench oil.Art technology
Personnel according to GB/T 9168-1997, can control the parameter of vacuum distillation tower, obtain the above-mentioned cut point of cracked oil, so as to control
The composition of quench oil.
Floating bed hydrogenation reactor in the processing system of this pyrolysis oil gas, catalyst 15 used are catalyzed for solid particle
Agent, such as one or more in solid particle catalyst selection iron containing compoundses, the oxide of ferrum, the sulfate of ferrum, the sulfur of ferrum
Compound, ferrum it is muriatic one or more；Can also be the form of mineral dust, such as pyrite, red mud, bloodstone, laterite
One or more in type nickel minerals, limonite, catalyst particle size scope are 5～10 μm, and addition accounts for reaction raw materials gross weight
0.1～5.0%, preferably 0.5～3.0%.
Using above-mentioned processing system, the method for reclaiming and processing pyrolysis oil gas, body are comprised the following steps：
Chilling：Pyrolysis oil gas obtains condensing heavy oil and cooling oil gas under the spray effect of cooling oil；
Air-distillation：Cooling oil steam distillation obtains pyrolysis gas and normal pressure bottom of tower heavy oil；
It is hydrocracked：Normal pressure bottom of tower heavy oil generates hydrogenation products in the presence of catalyst and hydrogen；
Gas-liquid separation：Hydrogenation products are isolated to cracked gas and cracked oil；
Vacuum distillation：By cracked oil vacuum distillation, quench oil and VACUUM TOWER BOTTOM heavy oil, quench oil supply quencher are obtained；
Gas is separated：Cracked gas and pyrolysis gas are carried out gas to separate, hydrogen and fuel gas is obtained.
In order to remove the large granular impurity in pyrolysis gas, also include the step of pyrolysis oil gas dedusting before chilling step；
In order to protect air-distillation equipment, also include the step of stably cooling down oil gas before air-distillation step.
For save energy, the side-product that this utility model cyclic utilization system is produced, such as：
The condensation heavy oil that chilling step is obtained is admitted to floating bed hydrogenation reactor and is hydrocracked；
Or, the VACUUM TOWER BOTTOM heavy oil obtained by vacuum distillation is admitted to into floating bed hydrogenation reactor and is hydrocracked；
Or, the quench oil obtained by vacuum distillation is admitted to atmospheric distillation tower carries out air-distillation；
Or, the hydrogen that gas trap is isolated is admitted in floating bed hydrogenation reactor.
Specifically, as shown in Fig. 2 the method for work of the processing system of this utility model pyrolysis oil gas includes：
(1) self-pyrolysis stove pyrolysis oil gas out enters pyrolysis oil gas after entering the mechanical admixtures such as cleaner unit, removing dust
Quenching unit, is pyrolyzed oil gas in quenching unit by the part quench oil Quench from vacuum distillation, obtains condensation heavy oil and just
Cold oil gas；
(2) just cold oil gas Jing after regulator into atmospheric distillation tower isolate pyrolysis gas, naphtha cut, diesel oil distillate,
Bottom of tower heavy oil；
(3) the condensation heavy oil mixing of bottom of tower heavy oil and quenching unit is being urged as the raw material of floating bed hydrocracking unit
In the presence of agent and hydrogen, coal tar heavies enter gas-liquid separation unit Jing after slurry-bed hydrocracking, separate
Go out cracked gas and cracked oil；
(4) cracked oil into vacuum distillation tower isolate overhead light-end (≤500 DEG C of fractions) and bottom of tower heavy oil (>500℃
Fraction), light fraction is partly into pyrolysis gas quenching unit, raw material of the part as atmospheric distillation tower, tower as quench oil
Bottom heavy oil partial loops back floating bed hydrocracking unit, and part is outer to get rid of；
(5) cracked gas and pyrolysis gas enter gas separation unit, and the hydrogen isolated is used as floating bed hydrocracking unit
Hydrogen source, other gases are used as fuel gas.
This utility model is pyrolyzed the processing system of oil gas, and fast pyrogenation oil gas is entered atmospheric distillation tower Jing after just cold, point
Pyrolysis gas component, naphtha cut, diesel oil distillate and normal pressure heavy component are separated out, normal pressure heavy component carries out floating bed hydrogenation
Cracking reaction, Jing after gas-liquid separation, liquid phase enters vacuum distillation tower, isolates light fraction and heavy distillat, a part of conduct of light fraction
Oil gas of the chilling oil cooling from pyrolysis oven, a part are fed as atmospheric tower, and heavy distillat part loops back floating bed hydrogenation
Reactor, cracked gas and pyrolysis gas enter gas trap, isolate hydrogen and other gases, and hydrogen is used as floating bed hydrogenation
Hydrogen source, other gases are used as fuel gas.
Below with embodiment describing this utility model in detail, but therefore embodiment does not limit of the present utility model
Use range.Specific embodiment is reclaimed and is processed in the low-order coal fast pyrogenation generation of Hunchun according to technological process shown in Fig. 1
Coalite tar.
Using Huichun Station of Jilin Province low-order coal as pyrolysis feed coal, its main property property is shown in Table 1 to this utility model.
1 Hunchun low-order coal main character of table
Embodiment 1
Oil gas from pyrolysis oven is cooled to 380 DEG C in pyrolysis gas quenching unit, is entered with 375 DEG C Jing after regulator is stable
Enter atmospheric distillation tower, pyrolysis gas are isolated at top, side line isolates naphtha cut, diesel oil distillate, it is normal pressure bottom of tower heavy oil, first cold
The charging of heavy oil and VACUUM TOWER BOTTOM heavy oil as floating bed hydrocracking unit, 420 DEG C of slurry-bed hydrocracking temperature, pressure
Power 12Mpa, catalyst are laterite-type nickel ore powder particle, and particle diameter is 5～10 μm, addition 2.0%, reaction primary product distribution
It is shown in Table 2.From table 2, green coke amount only has 0.5%, and light oil (naphtha cut and diesel oil distillate summation) yield is 88.3%.
Embodiment 2
Oil gas from pyrolysis oven is cooled to 400 DEG C in pyrolysis gas quenching unit, is entered with 385 DEG C Jing after regulator is stable
Enter atmospheric distillation tower, pyrolysis gas are isolated at top, side line isolates naphtha cut, diesel oil distillate, it is normal pressure bottom of tower heavy oil, first cold
The charging of heavy oil and VACUUM TOWER BOTTOM heavy oil as floating bed hydrocracking unit, 480 DEG C of slurry-bed hydrocracking temperature, pressure
Power 25Mpa, catalyst are red mud powder particle, and particle diameter is 10 μm, addition 3.0%, and reaction primary product distribution is shown in Table 2.By
Table 2 is visible, and 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 in pyrolysis gas quenching unit, is entered with 360 DEG C Jing after regulator is stable
Enter atmospheric distillation tower, pyrolysis gas are isolated at top, side line isolates naphtha cut, diesel oil distillate, it is normal pressure bottom of tower heavy oil, first cold
The charging of heavy oil and VACUUM TOWER BOTTOM heavy oil as floating bed hydrocracking unit, 470 DEG C of slurry-bed hydrocracking temperature, pressure
Power 20Mpa, catalyst are laterite-type nickel ore and red mud powder particle (respectively account for 50%, mass fraction, similarly hereinafter), and particle diameter is 7 μm, plus
Enter amount 0.5%, reaction primary product distribution is shown in Table 2.From table 2, green coke amount is 0.85%, and light oil yield is 88.1%.
Embodiment 4
Oil gas from pyrolysis oven is cooled to 350 DEG C in pyrolysis gas quenching unit, is entered with 345 DEG C Jing after regulator is stable
Enter atmospheric distillation tower, pyrolysis gas are isolated at top, side line isolates naphtha cut, diesel oil distillate, it is normal pressure bottom of tower heavy oil, first cold
The charging of heavy oil and VACUUM TOWER BOTTOM heavy oil as floating bed hydrocracking unit, 380 DEG C of slurry-bed hydrocracking temperature, pressure
Power 10Mpa, catalyst are limonite powder particle, and particle diameter is 10 μm, addition 5%, and reaction primary product distribution is shown in Table 2.By
Table 2 is visible, and 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 in pyrolysis gas quenching unit, is entered with 385 DEG C Jing after regulator is stable
Enter atmospheric distillation tower, pyrolysis gas are isolated at top, side line isolates naphtha cut, diesel oil distillate, it is normal pressure bottom of tower heavy oil, first cold
The charging of heavy oil and VACUUM TOWER BOTTOM heavy oil as floating bed hydrocracking unit, 400 DEG C of slurry-bed hydrocracking temperature, pressure
Power 9Mpa, catalyst are laterite nickel (30%) and pyrite (70%) powder particle, and particle diameter is 8 μm, addition 0.1%, reaction
Primary product distribution is shown in Table 2.From table 2, green coke amount is 0.68%, and light oil yield is 88.0%.
Comparative example 1
Atmospheric distillation tower is entered Jing after regulator is stable from the pyrolysis oil gas of pyrolysis oven is direct, tower top isolates pyrolysis
Gas, side line isolate naphtha cut, diesel oil distillate and bottom of tower heavy oil, and bottom of towe arranges the backflow of tower top heavy oil,
Cooling medium of the heavy oil backflow as pyrolysis oil gas, reaction primary product distribution are shown in Table 2.From table 2, this contrast
In example, green coke amount is 17.3%, and mainly in air-distillation tower bottom green coke, light oil yield also only has 68.3%.Highlight this reality
The advantage of atmospheric distillation tower is entered back into after being cooled down at the beginning of with novel pyrolytic oil gas is first.
Comparative example 2
From the cooling recovery method of pyrolysis oil gas coal-tar middle oil and coal gas using conventional coking process of pyrolysis oven, i.e. tar
After being cooled completely as floating bed hydrocracking unit raw material, floating bed hydrogenation operation condition is same as Example 1,
Floating bed hydrogenation product enters vacuum distillation tower, and the light components isolated enter air-distillation unit, and heavy component is followed
Loopback floating bed hydrogenation reactor, reaction primary product distribution are shown in Table 2.
From table 2, after the coal-tar middle oil cooling completely of this comparative example, floating bed hydrocracking raw material, the increase of energy consumption are re-used as
It is it will be apparent that in addition compared with Example 1, the yield of naphtha cut and diesel oil distillate is significantly reduced, light oil yield
Reduce by 12.4 percentage points.
2 embodiment of table and the distribution of comparative example primary product
What this utility model disclosure was touched upon is exemplary embodiment, in the protection defined without departing from claims
In the case of scope, each embodiment of the present utility model can be made various changes and modifications.Therefore, described enforcement
Example is intended to all such changes, modifications and deformation in the protection domain of appended claims.Additionally, except upper and lower
Outside text refers else, the word for occurring in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then appoint
All or part of of what embodiment can be with reference to all or part of use of any other embodiment.
Claims (8)
1. it is a kind of pyrolysis oil gas processing system, it is characterised in that include：
Quencher, is provided with pyrolysis oil gas entrance, chilling oil-in, cooling oil gas vent and condensation heavy oil outlet；
Atmospheric distillation tower, is provided with cooling oil gas entrance, pyrolysis gas outlet, chilling oil-in and heavy oil outlet；The cooling oil
Gas entrance is connected with the cooling oil gas vent of the quencher；
Floating bed hydrogenation reactor, is provided with heavy oil entrance, hydrogenation products outlet, hydrogen inlet；The heavy oil entrance is normal with described
The heavy oil outlet connection of pressure distillation column；
Gas-liquid separator, is provided with hydrogenation products entrance, cracking gas exit and cracking oil export；The hydrogenation products entrance with it is described
The hydrogenation products outlet connection of floating bed hydrogenation reactor；
Vacuum distillation tower, is provided with cracking oil-in, chilling oil export and circulation heavy oil outlet；The cracking oil-in and the gas
The cracking oil export connection of liquid/gas separator；The chilling oil export is connected with the chilling oil-in of the quencher；
Gas trap, is provided with pyrolysis gas entrance, cracked gas entrance, hydrogen outlet；The pyrolysis gas entrance is steamed with the normal pressure
Evaporate the pyrolysis gas outlet connection of tower；The cracked gas entrance is connected with the cracking gas exit of the gas-liquid separator.
2. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that the condensation heavy oil outlet of the quencher
It is connected with the heavy oil entrance of the floating bed hydrogenation reactor.
3. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that the chilling of the vacuum distillation tower
Oil export is connected with the chilling oil-in of the atmospheric distillation tower.
4. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that the circulation heavy oil of the vacuum distillation tower
Outlet is connected with the heavy oil entrance of the floating bed hydrogenation reactor.
5. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that the hydrogen outlet of the gas trap
It is connected with the hydrogen inlet of the floating bed hydrogenation reactor.
6. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that further include cleaner unit, it is described to remove
The pyrolysis oil gas entrance of the outlet connection quencher of dirt device.
7. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that further include regulator, it is described steady
The air intake for determining device connects the cooling oil gas vent of the quencher, and the gas outlet of the regulator connects the atmospheric distillation tower
Cooling oil gas entrance.
8. the processing system of oil gas is pyrolyzed as claimed in claim 1, it is characterised in that the quench oil is that cracked oil Jing reduces pressure
Distillation obtain≤500 DEG C of light fraction.
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| CN201620683944.8U CN206051957U (en) | 2016-07-01 | 2016-07-01 | A kind of processing system of pyrolysis oil gas |
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| CN201620683944.8U CN206051957U (en) | 2016-07-01 | 2016-07-01 | A kind of processing system of pyrolysis oil gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950227A (en) * | 2016-07-01 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Treatment system and method for pyrolyzed oil gas |
| CN109737420A (en) * | 2018-12-27 | 2019-05-10 | 怀集汇清环保设备工程有限公司 | A kind of house refuse back-fire type pyrolysis disposing technique and device |
-
2016
- 2016-07-01 CN CN201620683944.8U patent/CN206051957U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950227A (en) * | 2016-07-01 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Treatment system and method for pyrolyzed oil gas |
| CN109737420A (en) * | 2018-12-27 | 2019-05-10 | 怀集汇清环保设备工程有限公司 | A kind of house refuse back-fire type pyrolysis disposing technique and device |
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