CN206051943U - A kind of low-order coal is pyrolyzed oil and gas processing combined system - Google Patents
A kind of low-order coal is pyrolyzed oil and gas processing combined system Download PDFInfo
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- CN206051943U CN206051943U CN201620687208.XU CN201620687208U CN206051943U CN 206051943 U CN206051943 U CN 206051943U CN 201620687208 U CN201620687208 U CN 201620687208U CN 206051943 U CN206051943 U CN 206051943U
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Abstract
This utility model discloses a kind of low-order coal pyrolysis oil and gas processing combined system.The system includes：Quencher, atmospheric distillation tower, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device, gas are separated and depurator and ethylene glycol synthesis system；The cooling oil gas vent connection atmospheric distillation tower of quencher, the heavy oil outlet of atmospheric distillation tower are sequentially connected floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device, gas and separate and depurator and ethylene glycol synthesis system.Heavy residue oil after this utility model deep vacuum distillation is not recycled to floating bed hydrogenation reactor, it is to avoid the coking during floating bed hydrogenation.By gas generation ethylene glycol obtained by residue oil, the motility of heavy component processing is improve, improve process economy.
Description
Technical field
This utility model belongs to a kind of pyrogenous origin oil of low-order coal, the combined system of gas processing.In particular, it is to relate to
And one kind is during coal fast pyrogenation, couple tar, pyrolysis gas recovery and processing, production light-weight fuel oil and ethylene glycol is
System.
Background technology
China accounts for more than 55% for low-order coal (such as jet coal, brown coal etc.) in having verified coal reserves, the coalification of low-order coal
Low degree, volatile matters are high, water content is high, and directly burning or gasification efficiency are low.The utilization of low-order coal is faced, prior art proposes to divide
The Technology that matter is utilized.
Coal sub-prime is using being considered as effective way that low-order coal clean and effective is utilized, and China " 13 " coalification
The direction that work is given priority to.The sub-prime of coal is wrapped using being exactly first to separate heterogeneity in coal by pyrolysises
Include coal gas, tar and semicoke for finally giving etc..Wherein, can be used as raw material or fuel after gas purification；Coal tar is by adding
Hydrogen can produce gasoline, diesel oil；Semicoke becomes the clean fuel of low volatile, low-sulfur by pyrolysis, for generating electricity, gasifying
Deng.
" tap " that coal sub-prime is utilized is the pyrolytic technique of coal, and pyrolytic technique is exactly to extract the tar of scale production quantities, coal
Gas.With the progress of science and technology, using needing scale, maximizing, single set pyrolysis of coal unit scale is more and more large-scale for coal sub-prime,
And pyrolysis rate is also improved rapidly, even only several seconds response time of the coal in pyrolysis oven, pyrolysis oil gas overflow speed soon,
And the coal tar of output mostly is middle coalite tar, its property has bigger difference with the coal tar of conventional coking output.
During the sub-prime of low-order coal is utilized, the comprehensive utilization one chemical industry for imitating the preferential, system integration is carried in order to embody
Skill process a, wherein comprehensive Utilization Ways are：Pyrolysis-oil gas upgrading-coal-char combustion-generating.Rich in an oxidation in pyrolysis gas
Carbon, hydrogen and other lower carbon number hydrocarbons classes, coal tar belong to containing the higher middle coalite tar of light component, but the heat of rapid pyrolysis oil
Less stable, heavy component are easy to be condensed green coke during freshening repeatedly.
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.
Existing another kind prepares the technique of PTA/PET based on pyrolysis gasifying device, and the technique is with Coal Gasification as core system
Standby coal base PTA/PET, including coal tar hydrorefining unit, Petroleum refined unit, methanol synthesis unit, methanol-Petroleum
Reformation/coupling unit, ethylene glycol synthesis unit etc., comprise the concrete steps that coal first passes through pyrolysis and obtains raw coke oven gas and semicoke, raw coke oven gas
Gas solid separation is carried out, and dedusting coal gas carries out gas-liquid separation again, synthesis gas separator entered after pyrolysis gas purification, and after water-cooled, tar enters
Row oil-water separation, purification tar obtain aromatic hydrocarbons and Petroleum through Aromatics Extractive Project, hydrofinishing, and semicoke carries out high-temperature gasification production
Synthesis gas, the pyrolysis gas and char Gasification gas after purification as follow-up chemical products synthetic raw gas, with synthesize Petroleum, first
Alcohol, ethylene glycol finally synthesize PTA/PET for raw material.
The conversion of coal in the technique has coupled pyrolysis and gasification, and this kind of technique is typically former as pyrolysis from fine coal
Material, pyrolysis oil air cooling are reclaimed and adopt traditional method, need oil-water separation, and tar is high with the emulsifying degree of water.Additionally, coal tar
In usually contain more coal dust and coal ash, and heavy component is also more, carries out Aromatics Extractive Project to full fraction coal tar, at raw material
Reason amount is big, and high energy consumption, yield are low；Hydrofinishing process, the lighting low degree of coal tar, heavy component are carried out to coal tar only
Can not be fully used.
Utility model content
The purpose of this utility model is to provide a kind of utilization low-order coal pyrolysis production of hydrocarbons light Fuel and ethylene glycol
System, it is to avoid the heavy component freshening green coke of pyrolysis oil gas, makes full use of pyrolysis oil gas, improves the economy of technique.
In order to realize foregoing invention purpose, this utility model discloses a kind of low-order coal pyrolysis oil and gas processing combined system, is
System includes：Quencher, atmospheric distillation tower, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device, gas
Body is separated and depurator and ethylene glycol synthesis system；The quencher is provided with cooling oil gas vent；The atmospheric distillation tower is provided with
Cooling oil gas entrance, heavy oil outlet and light Fuel outlet；The cooling oil gas entrance is gone out with the cooling oil gas of the quencher
Mouth connection；The floating bed hydrogenation reactor is provided with heavy oil entrance, hydrogenation products outlet；The heavy oil entrance connects the normal pressure
The heavy oil outlet of distillation column；The gas-liquid separator is provided with hydrogenation products entrance and cracking oil export；The hydrogenation products entrance
It is connected with the hydrogenation products outlet of the floating bed hydrogenation reactor；The vacuum distillation tower is provided with cracking oil-in, residue oil
Outlet；The cracking oil-in is connected with the cracking oil export of the gas-liquid separator；The residual oil gasification device is provided with residue oil
Entrance and syngas outlet；The residue oil-in is connected with the residue oil export of the vacuum distillation tower；The gas is separated
And depurator is provided with the outlet of synthesis gas entrance, hydrogen outlet and carbon monoxide；The synthesis gas entrance and the residual oil gasification device
Syngas outlet connection；The ethylene glycol synthesis system is provided with carbon monoxide inlet and hydrogen inlet；The carbon monoxide enters
Mouth separate with the gas and depurator carbon monoxide outlet；The hydrogen inlet is separated with the gas and depurator
Hydrogen outlet connection.
According to concrete preferred implementation of the present utility model, the quencher is provided with condensation heavy oil outlet, the condensation
Heavy oil outlet is connected with the heavy oil entrance of the floating bed hydrogenation reactor.
Or, the vacuum distillation tower is provided with chilling oil export, and the quencher is provided with chilling oil-in, and the normal pressure steams
Evaporate tower and be provided with chilling oil-in, chilling oil-in of the chilling oil export with the quencher, the urgency of the atmospheric distillation tower
Cold oil entrance connects.
The fraction less than 500～560 DEG C that cracked oil Jing vacuum distillations are obtained is sent into quencher by the vacuum distillation tower
Spray as pole cold oil.
Or, the atmospheric distillation tower is provided with pyrolysis gas outlet, and the gas is separated and depurator is provided with pyrolysis gas entrance,
The pyrolysis gas outlet connects the pyrolysis gas entrance of the gas separation and depurator.
Or, the gas-liquid separator is provided with cracking gas exit, and the gas is separated and depurator is provided with cracked gas entrance,
The cracking gas exit connects the cracked gas entrance of the gas separation and depurator.
Or, the floating bed hydrogenation reactor is provided with hydrogen inlet, the hydrogen inlet of the floating bed hydrogenation reactor
Connect the hydrogen outlet of the gas separation and depurator.
Or, the system further includes cleaner unit, the pyrolysis oil of the outlet connection quencher of the cleaner unit
Gas entrance.
Or, the system further includes regulator, and the air intake of the regulator connects the cooling of the quencher
Oil gas vent, the gas outlet of the regulator connect the cooling oil gas entrance of the atmospheric distillation tower.
Wherein, the catalyst used by the floating bed hydrogenation reactor is containing one or more gold in Mo, Ni, Co, W, Fe
The homogeneous or heterogeneous catalysis of category.
The homogeneous catalyst includes one or more in naphthenate, soap, metal complex, wherein, with
Metallic element is measured, and the tenor is 50～200 μ g/g；Preferably 80～150 μ g/g.
And the heterogeneous catalysis is to include lateritic nickel ore, red mud, or the useless agent of fixed bed hydrogenation one or more mixed
Compound, addition are the 0.1～5.0% of the gross weight of the floating bed hydrogenation reactor content；Preferably 0.5～3.0%.
Heavy residue oil after this utility model this utility model deep vacuum distillation is not recycled to floating bed hydrogenation reactor, keeps away
The coking during floating bed hydrogenation is exempted from；Residue oil is carried out into catalytic gasification, is made after gasification gas and the purified separation of pyrolysis gas
To produce the raw material of ethylene glycol, the motility of coal tar heavy component processing is improve, improve process economy；In addition, this reality
With the decompression light fraction part of new employing floating bed hydrogenation product as the cooling medium of pyrolysis oil gas, partly steam as normal pressure
Tower charging, the cooling medium better heat stability, it is to avoid the secondary condensation green coke in cooling procedure are evaporated, while avoiding water-cooled product
The substantial amounts of phenol-containing wastewater of life, can improve light oil yield；And the advanced row quenching of oil gas is pyrolyzed, by the heavy tar in oil gas
Cool down, the tar and pyrolysis gas of relative lightweight enter atmospheric distillation tower, continue separate out light ends, can make full use of
First cold oil gas heat, it is to avoid redistilled energy consumption after cooling down completely；The hydrogen that pyrolysis gas are isolated is used for coal tar heavy group
Divide floating bed hydrocracking, realize the self-sufficiency of hydrogen, save hydrogen manufacturing cost.
Description of the drawings
Fig. 1 is the schematic diagram that this utility model is pyrolyzed oil and gas processing combined system embodiment；
Fig. 2 is the schematic diagram that this utility model is pyrolyzed oil and gas processing combined method embodiment.
2 description of symbols of accompanying drawing
1st, it is pyrolyzed oil gas, 2, cleaner unit, 3, oil gas 4, quencher after dedusting, 5, first cold oil gas, 6, regulator, 8, normal pressure steams
Evaporate tower, 9, pyrolysis gas, 10, naphtha cut, 11, diesel oil distillate, 12, normal pressure bottom of tower heavy oil, 13, condensation heavy oil fraction, 14, urge
Agent, 15, floating bed hydrogenation reactor, 16, floating bed hydrogenation product, 17, gas-liquid separator, 18, cracked gas, 19, cracked oil,
20th, vacuum distillation tower, 21,22,23, quench oil, 24, VACUUM TOWER BOTTOM residue oil, 25, residual oil gasification device, 26, gasification gas, 27, gas
Body is separated and depurator, 28,29, hydrogen, 30, carbon monoxide, 31, other lower carbon number hydrocarbons, 32, ethylene glycol synthesis technique system, 33,
Ethylene glycol, 34, other products
Specific embodiment
This utility model discloses a kind of low-order coal pyrolysis oil and gas processing combined system, will pyrolysis oil gas Jing chillings, normal pressure steaming
Evaporate, cracking separation, deep vacuum distillation, gained heavy component is not recycled to floating bed hydrogenation reactor, it is to avoid floating bed hydrogenation mistake
Coking in journey；Residue oil is gasified, and gained synthesis gas is separated and purified, and isolates carbon monoxide, hydrogen as synthesis second
The raw material of glycol, improves the motility of pyrolysis oil gas heavy component processing, improves process economy.
Specifically, this utility model discloses a kind of low-order coal pyrolysis oil and gas processing combined system, is using heavy coal tar
Quench oil of the part light components after floating bed hydrogenation as pyrolysis oil gas, partly as the charging of atmospheric distillation tower, condensation
The raw material of heavy tar, atmospheric tower bottom heavy tar as floating bed hydrocracking, VACUUM TOWER BOTTOM heavy tar carry out vaporizing system
Synthesis gas, pyrolysis gas, cracked gas, heavy tar gasification synthesis gas are separated and are purified through gas, isolate carbon monoxide, hydrogen
And other lower carbon number hydrocarbons, the raw material of carbon monoxide, hydrogen as synthesizing glycol, while hydrogen partial is floating bed hydrogenation reaction carrying
Hydrogen source, other lower carbon number hydrocarbons are used as pyrolysis oven fuel gas.
Low-order coal pyrolysis oil and gas processing combined system disclosed in this utility model, system include：Quencher, air-distillation
Tower, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device, gas are separated and depurator and ethylene glycol
Synthesis system.Wherein, quencher is provided with cooling oil gas vent；Atmospheric distillation tower is provided with cooling oil gas entrance and heavy oil is exported and light
Matter fuel outlet；Cooling oil gas entrance is connected with the cooling oil gas vent of quencher；Floating bed hydrogenation reactor is provided with heavy oil and enters
Mouth, hydrogenation products outlet；The heavy oil outlet of heavy oil entrance connection atmospheric distillation tower；Gas-liquid separator be provided with hydrogenation products entrance and
Cracking oil export；Hydrogenation products entrance is connected with the hydrogenation products outlet of floating bed hydrogenation reactor；Vacuum distillation tower is provided with and splits
Carburetion entrance, residue oil export；Cracking oil-in is connected with the cracking oil export of gas-liquid separator；Residual oil gasification device is provided with residue
Oil-in and syngas outlet；Residue oil-in is connected with the residue oil export of vacuum distillation tower；Gas is separated and depurator sets
There is the outlet of synthesis gas entrance, hydrogen outlet and carbon monoxide；Synthesis gas entrance is connected with the syngas outlet of residual oil gasification device；Second
Glycol synthesis system is provided with carbon monoxide inlet and hydrogen inlet；Carbon monoxide inlet separate with gas and depurator an oxidation
Carbon outlet；Hydrogen inlet is separated with gas and the hydrogen outlet of depurator connects.
Heavy residue oil after this utility model deep vacuum distillation is not recycled to floating bed hydrogenation reactor, it is to avoid suspension bed
Coking in hydrogenation process；Residue oil is carried out into catalytic gasification, as the raw material for producing ethylene glycol after the purified separation of gas of gasifying,
The motility of coal tar heavy component processing is improve, process economy is improved.
This utility model is not excluded for recycling the intermediate product of the system, with save energy, improves efficiency, will such as subtract
Quench oil of the light components of pressure distillation gained as quencher, and the pan feeding of air-distillation, cyclic process；By obtained by chilling
Heavy component sends into floating bed hydrocracking；Or by the separating obtained cracked gas of pyrolysis gas, hydrogenation products obtained by air-distillation, with
Synthesis gas isolation of purified together；Hydrogen obtained by isolation of purified sends into suspension bed etc..
Fig. 1 is the schematic diagram of a preferred embodiment of this utility model pyrolysis oil and gas processing combined system, refer to Fig. 1,
The present embodiment low-order coal pyrolysis oil and gas processing combined system includes：It is cleaner unit 2, quencher 4, regulator 6, atmospheric distillation tower 8, outstanding
Floating bed hydrogenation reactor 15, gas-liquid separator 17, vacuum distillation tower 20, residual oil gasification device 25, gas are separated and 27 and of depurator
Ethylene glycol synthesis system 32.
Said apparatus connected mode is：
Pyrolysis outlet of still is connected with the entrance of cleaner unit 2.Pyrolysis coal gas 1 directly from pyrolysis oven out is entered by cleaner unit 2
Row dust removal process, removes the mechanical admixture such as dust in pyrolysis coal gas, obtains oil gas 3 after dedusting.
Quencher 4 is provided with pyrolysis oil gas entrance, chilling oil-in, the outlet of condensation heavy oil and cools down oil gas vent.Pyrolysis oil
Gas entrance connects the outlet of cleaner unit 2, and after dedusting, oil gas 3 carries out chilling into quencher 4 by cleaner unit 2 and operates, and obtains just cold
Oil gas 5.
Regulator 6 is provided with air intake and gas outlet.Air intake connects the cooling oil gas vent of quencher 4.Just cold oil gas 5 enters
Enter regulator 6, by the steady air current of first cold oil gas 5, it is to avoid because air-flow shakiness causes damage to next device.
Atmospheric distillation tower 8 is provided with cooling oil gas entrance, heavy oil outlet, light Fuel outlet and pyrolysis gas outlet.Regulator 6
Gas outlet connect the cooling oil gas entrance of atmospheric distillation tower 8, will it is stable after cooling oil pneumatic transmission enter and carry out in atmospheric distillation tower 8
Reaction, obtains pyrolysis gas 9, light Fuel and bottom of tower heavy oil 12.The light Fuel that atmospheric distillation tower is produced is divided into naphtha cut
10 and diesel oil distillate 11, light Fuel outlet is also accordingly divided into naphtha cut outlet and diesel oil distillate is exported.
Floating bed hydrogenation reactor 15 is provided with the outlet of heavy oil entrance, hydrogen inlet and hydrogenation products.The connection of heavy oil entrance is normal
The heavy oil outlet of pressure distillation column 8 and the condensation heavy oil of quencher are exported, and carry out cracking anti-in the presence of hydrogen 28 and catalyst converter
Should, obtain hydrogenation products 16.
Gas-liquid separator 17 is provided with hydrogenation products entrance, cracking gas exit and cracking oil export.Hydrogenation products entrance connects
The hydrogenation products outlet of floating bed hydrogenation reactor 15, hydrogenation products 16 are into 17 detached cracked gas 18 of gas-liquid separator and split
Carburetion 19.
Vacuum distillation tower 20 is provided with cracking oil-in, chilling oil export and residue oil export.Cracking oil-in connects gas-liquid
The cracking oil export of separator 17, cracked oil 19 are admitted to vacuum distillation tower 20 and carry out vacuum distillation, obtain the residual of heavy component
Residual oil 24 and light components 21.Chilling oil export connects the chilling oil-in of quencher 4 and the quench oil of atmospheric distillation tower 8 respectively
Entrance.A part for light components is admitted to quencher 4 as quench oil, and a part sends into atmospheric distillation tower 8 as raw material, often
The cooling oil gas entrance of pressure distillation column 8 and chilling oil-in can be same entrance, as feed(raw material)inlet.
Residual oil gasification device 25 is provided with residue oil-in and syngas outlet.Residue oil-in connects the residual of vacuum distillation tower 20
Residual oil is exported.Residue oil 24 is gasified into residual oil gasification device 25 by vacuum distillation tower 20, generates synthesis gas 26.
Gas is separated and depurator 27 is provided with synthesis gas entrance, pyrolysis gas entrance, cracked gas entrance, hydrogen outlet and an oxygen
Change carbon outlet and fuel gas is exported.The syngas outlet of synthesis gas entrance connection residual oil gasification device 25.The connection of pyrolysis gas entrance is normal
The pyrolysis gas outlet of pressure distillation column 8.Cracked gas entrance connects the cracking gas exit of gas-liquid separator 17.Residual oil gasification device 25 is produced
Synthesis gas, atmospheric distillation tower 8 produce pyrolysis gas, gas-liquid separator 17 produce cracked gas be admitted to gas separate and purify
Device 27, is separated, and obtains hydrogen 28, carbon monoxide 30 and fuel gas 31.
Ethylene glycol synthesis system 32 is provided with carbon monoxide inlet and hydrogen inlet, ethylene glycol outlet and other product exits.
Hydrogen inlet, carbon monoxide inlet connect gas separation and hydrogen outlet, the carbon monoxide outlet of depurator 27 respectively.Gas point
From and depurator 27 produce a part of hydrogen 28 and carbon monoxide 30 be admitted in ethylene glycol synthesis system 32 and synthesized, obtain
To ethylene glycol 33 and other products 34.
The hydrogen outlet of gas separation and depurator 27 also connects the hydrogen inlet of floating bed hydrogenation reactor 15.
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.
Catalyst used by this utility model floating bed hydrogenation reactor can be comprising a kind of in Mo, Ni, Co, W, Fe or
The homogeneous or heterogeneous catalysis of several metals.Homogeneous catalyst includes in naphthenate, soap, metal complex one
Plant or several, wherein, being measured with metallic element, tenor is 50～200 μ g/g；Preferably 80～150 μ g/g.
And heterogeneous catalysis can be to include lateritic nickel ore, red mud, or the useless agent of fixed bed hydrogenation one or more mixed
Compound, addition for the gross weight of floating bed hydrogenation reactor content 0.1～5.0%, preferably 0.5～3.0%.
This utility model residual oil gasification unit adopts part residue oil partial oxidation technology to generate with carbon monoxide and hydrogen
Based on raw material of synthetic gas, gasifying agent is oxygen and vapor, and wherein oxygen oil is than for 0.4～0.8 (m3/ kg is oily).
Gasification reaction using natural crystal as gasification auxiliary agent, such as one or more of dolomite, olivine, clay Ore,
Addition be 0.1～2.0% (mass percent of gasifier combined feed), preferably 0.2～1.5%.Gasification temperature 800～1100
DEG C, 0.1～5s of response time, preferably 0.5～3.0s.
Floating bed hydrogenation reaction condition is：400～485 DEG C of temperature, preferably 420～475 DEG C, 10～25Mpa of pressure, preferably
12～24Mpa.
Pyrolysis oil gas is cooled to 410～480 DEG C in pyrolysis gas quenching unit, preferably 420～460 DEG C, steams into normal pressure
The cooling oil temperature degree for evaporating tower is preferably 380～450 DEG C.
It should be noted that connection described in the utility model or connection, refer to pipeline or other equipment, by previous dress
The product for putting generation is sent in next device.
This utility model application said system, processes the method that combined treatment low-order coal is pyrolyzed oil gas, comprises the steps：
Chilling：Will be pyrolysis oil out of breath cold, generate cooling oil gas；
Air-distillation：Oil gas air-distillation will be cooled down, bottom of tower heavy oil and light Fuel will be obtained；
Cracking, gas-liquid separation：By bottom of tower heavy oil cracking, gas-liquid separation, cracked oil is obtained；
Vacuum distillation：Cracked oil vacuum distillation is obtained into residue oil；
Residual oil gasification：Residue oil gasification is obtained into synthesis gas；
Gas is separated and is purified：Synthesis gas is separated, is purified, obtain hydrogen, carbon monoxide；
Ethylene glycol synthesizes：By carbon monoxide and hydrogen synthesizing glycol.
In order to cost-effective, the side-product of generation is recycled by this utility model, while pyrolysis oil gas is made full use of, therefore
The method of this utility model low-order coal pyrolysis oil and gas processing combination can also include following either step, or multiple steps therein
Suddenly：
The condensation heavy oil that chilling step is generated is sent into floating bed hydrogenation reactor and carries out cracking；
The quench oil that vacuum distillation step is generated, sends into respectively as quench oil feeding chilling step, as raw material
Air-distillation；
The pyrolysis gas that air-distillation is generated are sent into gas separation and depurator and carry out the gas separation and purification；
The cracked gas that gas-liquid separation step is generated is sent into gas separation and depurator and carries out gas separation and purifying step；
The hydrogen partial that gas is separated and purifying step is obtained is sent into into the floating bed hydrogenation reactor ancillary cracking anti-
Should；
Especially, this utility model is also included the step of pyrolysis oil gas dedusting before chilling step.Or, walk in chilling
It is rapid also to include the step of stably cooling down oil gas and air-distillation step between.
Fig. 2 is the schematic diagram that this utility model is pyrolyzed oil and gas processing combined method embodiment, as shown in Fig. 2 the present embodiment
The method of low-order coal pyrolysis oil and gas processing combination is comprised the following steps：
(1) it is pyrolyzed after oil gas enters the mechanical admixtures such as cleaner unit, removing dust and enters pyrolysis gas quenching unit, in chilling list
Oil gas is pyrolyzed in unit by the part quench oil Quench from vacuum distillation, condensation heavy oil and first cold oil gas is obtained；
(2) just cold oil gas Jing after regulator into atmospheric distillation tower fractionate out 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 isolates light components and heavy component into vacuum distillation tower, light components as quench oil, one
Pyrolysis gas quenching unit is partially into, raw material of the part as atmospheric distillation tower, heavy residue oil ingredient enter residual oil gasification
Unit carries out gasification reaction；
(5) pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and cleaning system, isolate carbon monoxide, hydrogen
And other lower carbon number hydrocarbons, carbon monoxide, hydrogen are used as synthesizing glycol raw material, while hydrogen partial is provided for floating bed hydrogenation reaction
Hydrogen source, other lower carbon number hydrocarbons are used as pyrolysis oven fuel gas.
This utility model vacuum distillation unit carries out deep vacuum distillation, and light, heavy constituent cut point is controlled at 500～565 DEG C.Split
The light component fraction less than 500～560 DEG C that the vacuum distillation of carburetion Jing is obtained, a part go pyrolysis oil as quench oil
Gas, a part remove distillation column；Can be used as suspension bed hydrogenation catalyst after heavy oil gasification residue treatment.
Those skilled in the art can control decompression according to oil product vacuum distillation algoscopy standard GB/T 9168-1997
The parameter of distillation column, obtains the above-mentioned cut point of cracked oil, so as to control the composition of cracked oil, cracked gas.
Below with specific embodiment describing this utility model in detail, but therefore embodiment does not limit this practicality newly
The use range of type.Specific embodiment is produced according to technological process shown in Fig. 2, processed Hunchun low-order coal fast pyrogenation
Oil gas.
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
2 Hunchun coal pyrolysis gas composition of table
Embodiment 1
420 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 400 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 420 DEG C of slurry-bed hydrocracking temperature, pressure
12Mpa, catalyst are molybdenum naphthenate, are measured with metallic element, and tenor is 80 μ g/g, and vulcanizing agent is distillation sulphur powder, is added
80 μ g/g are measured, vacuum distillation is light, the cutting temperature of heavy constituent is 520 DEG C, and residue oil gasification auxiliary agent selects dolime, adds
Amount 0.3%, gasifying agent is vapor and oxygen, and than for 0.4,850 DEG C of gasification temperature, response time 0.8S, split pyrolysis gas oxygen oil
Activating QI, residual oil gasification gas enter gas and separate and purification systems, isolate carbon monoxide, hydrogen and other lower carbon number hydrocarbons, high-purity
Carbon monoxide, hydrogen send into ethylene glycol synthetic system.Primary product index is shown in Table 3.
Embodiment 2
440 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 420 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 450 DEG C of slurry-bed hydrocracking temperature, pressure
18Mpa, adds heterogeneous catalysis, selects the mixture of laterite nickel and red mud, and addition 0.5%, homogeneous catalyst are metal
Tungsten complex, with metallic element measure, tenor be 50 μ g/g, vulcanizing agent for distillation sulphur powder, 100 μ g/g of addition, decompression
Distillation is light, the cutting temperature of heavy constituent is 550 DEG C, and residue oil gasification auxiliary agent selects calcining olivine, addition 0.5%, gasification
Agent is vapor and oxygen, and oxygen oil ratio is 0.6,900 DEG C of gasification temperature, response time 1.2S, pyrolysis gas, cracked gas, residual oil gas
Activating QI enters gas and separates and purification systems, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, high-purity CO, hydrogen
Pneumatic transmission enters ethylene glycol synthetic system.Primary product index is shown in Table 3.
Embodiment 3
460 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 450 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 475 DEG C of slurry-bed hydrocracking temperature, pressure
24Mpa, adds the useless agent of heterogeneous catalysis fixed bed hydrogenation, addition 3%, vulcanizing agent to be distillation sulphur powder, and vacuum distillation is light, weight
The cutting temperature of component is 565 DEG C, and residue oil gasification auxiliary agent selects calcined clay ore deposit, and addition 1.5%, gasifying agent are vapor
And oxygen, than being 0.75,1000 DEG C of gasification temperature, response time 3.0S, pyrolysis gas, cracked gas, residual oil gasification gas are entered oxygen oil
Gas is separated and purification systems, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, and high-purity CO, hydrogen send into second
Glycol synthetic system.Primary product index is shown in Table 3.
Embodiment 4
410 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 380 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 400 DEG C of slurry-bed hydrocracking temperature, pressure
10Mpa, catalyst is the alkyl salt of Mo, the fatty acid of Co, the compositionss of the complex of Ni, is measured with metallic element, and metal contains
Measure as 200 μ g/g, vulcanizing agent is distillation sulphur powder, 80 μ g/g of addition, and vacuum distillation is light, the cutting temperature of heavy constituent is 500 DEG C,
Residue oil gasification auxiliary agent selects dolime and olivine, addition 2.0%, and gasifying agent is vapor and oxygen, and oxygen is oily to be compared
For 0.8,850 DEG C of gasification temperature, response time 0.5S, pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and purification body
System, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, and high-purity CO, hydrogen send into ethylene glycol synthetic system.Mainly
Product index is shown in Table 3.
Embodiment 5
480 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 430 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 485 DEG C of slurry-bed hydrocracking temperature, pressure
25Mpa, catalyst are red mud, and addition is the 5.0% of the gross weight of floating bed hydrogenation reactor content.Vulcanizing agent is Sublimed Sulfur
Powder, 80 μ g/g of addition, vacuum distillation is light, the cutting temperature of heavy constituent is 520 DEG C, and residue oil gasification auxiliary agent selects calcining white clouds
Stone, addition 0.3%, gasifying agent are vapor and oxygen, and oxygen oil ratio is 0.8,1100 DEG C of gasification temperature, response time 0.1S,
Pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and purification systems, isolate carbon monoxide, hydrogen and other are low
Carbon hydrocarbon, high-purity CO, hydrogen send into ethylene glycol synthetic system.Primary product index is shown in Table 3.
Embodiment 6
480 DEG C are cooled in pyrolysis oil gas quenching unit after pyrolysis oil gas removing dust unit dedusting, Jing regulators are stable
Atmospheric distillation tower is entered with 450 DEG C afterwards, pyrolysis gas are isolated at top, and side line isolates naphtha cut, diesel oil distillate, atmospheric tower
The charging of bottom heavy oil, first cold heavy oil as floating bed hydrocracking unit, 450 DEG C of slurry-bed hydrocracking temperature, pressure
20Mpa, catalyst are containing red mud, red mud addition for the gross weight of floating bed hydrogenation reactor content 0.1%, the fat of W, Fe
Fat hydrochlorate, tenor are 150 μ g/g.Vulcanizing agent is distillation sulphur powder, 80 μ g/g of addition, and vacuum distillation is light, heavy constituent is cut
Temperature is cut for 500 DEG C, residue oil gasification auxiliary agent selects dolime, addition 0.1%, gasifying agent to be vapor and oxygen,
Than being 0.6,800 DEG C of gasification temperature, response time 5S, pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and net oxygen oil
Change system, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, and high-purity CO, hydrogen send into ethylene glycol synthetic system.
Primary product index is shown in Table 3.
3 embodiment primary product of table is distributed
Disclosed in this utility model, low-order coal pyrolysis oil and gas processing combined system, is using the coal tar suspension bed hydrogenation of heavy
Quench oil of the part light components afterwards as pyrolysis oil gas, partly as the charging of atmospheric distillation tower, condensation heavy tar, often
Raw material of the pressure bottom of towe heavy tar as floating bed hydrocracking, VACUUM TOWER BOTTOM heavy tar carry out gasification preparing synthetic gas, are pyrolyzed
Gas, cracked gas, heavy tar gasification synthesis gas are separated and are purified through gas, isolate carbon monoxide, hydrogen and other low-carbon (LC)s
Hydrocarbon, carbon monoxide, hydrogen are used as synthesizing glycol raw material, while hydrogen partial provides hydrogen source for floating bed hydrogenation reaction, other
Lower carbon number hydrocarbons are used as pyrolysis oven fuel gas.
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 (9)
1. a kind of low-order coal is pyrolyzed oil and gas processing combined system, it is characterised in that include：Quencher, atmospheric distillation tower, suspension bed
Hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device, gas are separated and depurator and ethylene glycol synthesis system；
The quencher is provided with cooling oil gas vent；
The atmospheric distillation tower is provided with cooling oil gas entrance, heavy oil outlet and light Fuel outlet；It is described cooling oil gas entrance with
The cooling oil gas vent connection of the quencher；
The floating bed hydrogenation reactor is provided with heavy oil entrance, hydrogenation products outlet；The heavy oil entrance connects the normal pressure and steams
Evaporate the heavy oil outlet of tower；
The gas-liquid separator is provided with hydrogenation products entrance and cracking oil export；The hydrogenation products entrance is added with the suspension bed
The hydrogenation products outlet connection of hydrogen reactor；
The vacuum distillation tower is provided with cracking oil-in, residue oil export；The cracking oil-in and the gas-liquid separator
Cracking oil export connects；
The residual oil gasification device is provided with residue oil-in and syngas outlet；The residue oil-in and the vacuum distillation tower
Residue oil export connects；
The gas is separated and depurator is provided with the outlet of synthesis gas entrance, hydrogen outlet and carbon monoxide；The synthesis gas entrance
Connect with the syngas outlet of the residual oil gasification device；
The ethylene glycol synthesis system is provided with carbon monoxide inlet and hydrogen inlet；The carbon monoxide inlet and the gas point
From and depurator carbon monoxide outlet；The hydrogen inlet is separated with the gas and the hydrogen outlet of depurator connects
Connect.
2. the system as claimed in claim 1, it is characterised in that the quencher is provided with condensation heavy oil outlet, the condensation weight
Oil export is connected with the heavy oil entrance of the floating bed hydrogenation reactor.
3. the system as claimed in claim 1, it is characterised in that the vacuum distillation tower is provided with chilling oil export, the chilling
Device is provided with chilling oil-in, and the atmospheric distillation tower is provided with chilling oil-in, the urgency of the chilling oil export and the quencher
The chilling oil-in connection of cold oil entrance, the atmospheric distillation tower.
4. the system as claimed in claim 1, it is characterised in that the atmospheric distillation tower is provided with pyrolysis gas outlet, the gas
Separate and depurator is provided with pyrolysis gas entrance, the pyrolysis gas outlet connects the gas separation and the pyrolysis gas of depurator enter
Mouthful.
5. the system as claimed in claim 1, it is characterised in that the gas-liquid separator is provided with cracking gas exit, the gas
Separate and depurator is provided with cracked gas entrance, the cracking gas exit connects the gas separation and the cracked gas of depurator enters
Mouthful.
6. the system as claimed in claim 1, it is characterised in that the floating bed hydrogenation reactor is provided with hydrogen inlet, described
The hydrogen inlet of floating bed hydrogenation reactor connects the hydrogen outlet of the gas separation and depurator.
7. the system as claimed in claim 1, it is characterised in that the system further includes cleaner unit, the cleaner unit
The pyrolysis oil gas entrance of the outlet connection quencher.
8. the system as claimed in claim 1, it is characterised in that the system further includes regulator, the regulator
Air intake connects the cooling oil gas vent of the quencher, and the gas outlet of the regulator connects the cooling of the atmospheric distillation tower
Oil gas entrance.
9. system as claimed in claim 3, it is characterised in that cracked oil Jing vacuum distillations are obtained by the vacuum distillation tower
Fraction less than 500～560 DEG C is sent into quencher and is sprayed as pole cold oil.
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| CN201620687208.XU CN206051943U (en) | 2016-07-01 | 2016-07-01 | A kind of low-order coal is pyrolyzed oil and gas processing combined system |
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| CN201620687208.XU CN206051943U (en) | 2016-07-01 | 2016-07-01 | A kind of low-order coal is pyrolyzed oil and gas processing combined system |
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Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
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Denomination of utility model: Combined system and method for processing oil gas generated by pyrolysis of low rank coal Effective date of registration: 20180330 Granted publication date: 20170329 Pledgee: Tianfeng Securities Co.,Ltd. Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000247 |
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