CN105936834A - Combined system and method for processing oil gas generated by pyrolysis of low rank coal - Google Patents
Combined system and method for processing oil gas generated by pyrolysis of low rank coal Download PDFInfo
- Publication number
- CN105936834A CN105936834A CN201610515416.6A CN201610515416A CN105936834A CN 105936834 A CN105936834 A CN 105936834A CN 201610515416 A CN201610515416 A CN 201610515416A CN 105936834 A CN105936834 A CN 105936834A
- Authority
- CN
- China
- Prior art keywords
- gas
- oil
- entrance
- outlet
- pyrolysis
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
-
- 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 combined system and method for processing oil gas generated by pyrolysis of low rank coal. The system comprises a quench cooler, a normal pressure distillation column, a suspended bed hydrogenation reactor, a gas-liquid separator, a vacuum distillation tower, a residuum gasifying device, a gas separation and purification device, and a glycol synthesis system. The method comprises the following steps: quenching pyrolysis oil gas to generate cooled oil gas; subjecting cooled oil gas to normal pressure distillation to obtain heavy oil in the bottom of a distillation column and light fuel; cracking the heavy oil, separating gas and liquid to obtained cracked oil; subjecting cracked oil to vacuum distillation to obtain residual oil; gasifying the residual oil to obtain syngas; separating and purifying syngas to obtain hydrogen and carbon monoxide; and synthesizing carbon monoxide and hydrogen to obtain glycol. After vacuum deep extraction, the heavy residual oil is not returned to the suspended bed hydrogenation reactor, and thus the coking during the hydrogenation process in the suspended bed is avoided. The gas prepared from residual oil is used to produce glycol, the flexibility of heavy component processing is improved, and the economy of the technology is increased.
Description
Technical field
The invention belongs to the pyrogenous origin oil of a kind of low-order coal, the combined system of gas processing and method.More
Specifically, relating to a kind of during coal fast pyrogenation, coupling tar, pyrolysis gas reclaim and add
Work, produces light-weight fuel oil and the system and method for ethylene glycol.
Background technology
China has verified in coal reserves and accounted for more than 55% is low-order coal (such as jet coal, brown coal etc.), low
The degree of coalification of rank coal is low, volatile matter is high, water content is high, and directly burning or gasification efficiency are low.Face
The utilization of low-order coal, prior art proposes the Technology that sub-prime utilizes.
The utilization of coal sub-prime is considered as the effective way that low-order coal clean and effective 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
Middle heterogeneity is first separated, including the coal gas finally given, tar and semicoke etc..Wherein, coal
Gas can be as raw material or fuel after purifying；Coal tar can produce gasoline, diesel oil by hydrogenation；
Semicoke becomes the cleaning fuel of low volatile, low-sulfur by pyrolysis, is used for generating electricity, gasification etc..
" leading " that coal sub-prime utilizes is the pyrolytic technique of coal, and pyrolytic technique is extracted scale exactly and produced
The tar of amount, coal gas.Along with the progress of science and technology, coal sub-prime utilizes needs scale, maximization, single
Set pyrolysis of coal unit scale is more and more large-scale, and pyrolysis rate improves the most rapidly, and coal is in pyrolysis oven
Response time be even only several seconds, it is fast that pyrolysis oil gas overflows speed, and the coal tar of output mostly is
Middle coalite tar, its character has bigger difference with the coal tar of conventional coking output.
During the sub-prime of low-order coal utilizes, imitate preferential, the comprehensive utilization of the system integration to embody to carry
Using integral process process, wherein a comprehensive Utilization Ways is: pyrolysis-oil gas upgrading-coal-char combustion-
Generating.Rich in carbon monoxide, hydrogen and other lower carbon number hydrocarbons class in pyrolysis gas, coal tar belongs to containing light group
Dividing higher middle coalite tar, but the heat stability of rapid pyrolysis oil is poor, heavy component is instead
It is prone to be condensed green coke during multiple freshening.
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 another kind prepares the technique of PTA/PET based on pyrolysis gasifying device, and this technique is with coal gas
Turn to core and prepare coal base PTA/PET, including coal tar hydrorefining unit, Petroleum refined unit,
Methanol synthesis unit, methanol-naphtha reforming/coupling unit, ethylene glycol synthesis unit etc., concrete steps
Being that coal first passes through pyrolysis acquisition raw coke oven gas and semicoke, raw coke oven gas carries out gas solid separation, and dedusting coal gas enters again
Row gas-liquid separation, pyrolysis gas enters synthesis gas separator after purifying, and after water-cooled, tar carries out oil-water separation,
Purifying tar and obtain aromatic hydrocarbons and Petroleum through Aromatics Extractive Project, hydrofinishing, semicoke carries out high-temperature gasification
Produce synthesis gas, pyrolysis gas after purification and char Gasification gas as follow-up chemical products synthetic raw gas,
PTA/PET is finally synthesized with the Petroleum synthesized, methanol, ethylene glycol for raw material.
In this technique, the conversion of coal has coupled pyrolysis and gasification, and this kind of technique typically selects fine coal to make
For pyrolysis feed, pyrolysis oil air cooling reclaims and uses traditional method, needs oil-water separation, tar and water
Emulsifying degree high.Additionally, usually contain more coal dust and coal ash in coal tar, and heavy component
The most more, full fraction coal tar is carried out Aromatics Extractive Project, feed throughput is big, and energy consumption is high, and yield is low；
Only coal tar being carried out hydrofinishing process, the lighting degree of coal tar is low, and heavy component can not obtain
To making full use of.
Summary of the invention
It is an object of the invention to provide one and utilize low-order coal pyrolysis production of hydrocarbons light Fuel and second two
The system of alcohol and process, it is to avoid the heavy component freshening green coke of pyrolysis oil gas, make pyrolysis oil gas fill
Divide and utilize, improve the economy of technique.
In order to realize foregoing invention purpose, the open a kind of low-order coal pyrolysis oil and gas processing combination of the present invention is
System, system includes: quencher, atmospheric distillation tower, floating bed hydrogenation reactor, gas-liquid separator,
Vacuum distillation tower, residual oil gasification device, gas separate and depurator and ethylene glycol synthesis system；Described urgency
Cooler is provided with cooling oil gas vent；Described atmospheric distillation tower be provided with cooling oil gas entrance, heavy oil outlet and
Light Fuel exports；Described cooling oil gas entrance is connected with the cooling oil gas vent of described quencher；Institute
State floating bed hydrogenation reactor and be provided with heavy oil entrance, hydrogenation products outlet；Described heavy oil entrance connects institute
State the heavy oil outlet of atmospheric distillation tower；Described gas-liquid separator is provided with hydrogenation products entrance and cracked oil goes out
Mouthful；Described hydrogenation products entrance exports with the hydrogenation products of described floating bed hydrogenation reactor and is connected；Institute
State vacuum distillation tower and be provided with cracked oil entrance, residue oil outlet；Described cracked oil entrance and described gas-liquid
The cracked oil outlet of separator connects；Described residual oil gasification device is provided with residue oil entrance and syngas outlet；
Described residue oil entrance exports with the residue oil of described vacuum distillation tower and is connected；Described gas separates and clean
Change device and be provided with synthesis gas entrance, hydrogen outlet and carbon monoxide outlet；Described synthesis gas entrance is with described
The syngas outlet connection of residual oil gasification device；Described ethylene glycol synthesis system be provided with carbon monoxide inlet and
Hydrogen inlet；Described carbon monoxide inlet separates with described gas and the carbon monoxide outlet of depurator connects
Logical；Described hydrogen inlet separates with described gas and the hydrogen outlet of depurator connects.
According to particularly preferred embodiments of the invention, described quencher is provided with condensation heavy oil outlet, institute
State condensation heavy oil outlet to be connected with the heavy oil entrance of described floating bed hydrogenation reactor.
Or, described vacuum distillation tower is provided with quench oil outlet, and described quencher is provided with quench oil entrance,
Described atmospheric distillation tower is provided with quench oil entrance, the outlet of described quench oil and the quench oil of described quencher
Entrance, the quench oil entrance of described atmospheric distillation tower connect.
Or, described atmospheric distillation tower is provided with pyrolysis gas outlet, and described gas separates and depurator is provided with
Pyrolysis gas entrance, described pyrolysis gas outlet connects described gas and separates and the pyrolysis gas entrance of depurator.
Or, described gas-liquid separator is provided with cracking gas exit, and described gas separates and depurator is provided with
Cracked gas entrance, described cracking gas exit connects described gas and separates and the cracked gas entrance of depurator.
Or, described floating bed hydrogenation reactor is provided with hydrogen inlet, described floating bed hydrogenation reactor
Hydrogen inlet connect described gas separate and the hydrogen outlet of depurator.
Or, described system farther includes cleaner unit, and the outlet of described cleaner unit connects described chilling
The pyrolysis oil gas entrance of device.
Or, described system farther includes regulator, and the air intake of described regulator connects described urgency
The cooling oil gas vent of cooler, the gas outlet of described regulator connects the cooling oil of described atmospheric distillation tower
Gas entrance.
Wherein, the catalyst used by described floating bed hydrogenation reactor is containing Mo, Ni, Co, W, Fe
In the homogeneous or heterogeneous catalysis of one or more metals.
Described homogeneous catalyst includes the one in naphthenate, soap, metal complex or several
Kind, wherein, measuring with metallic element, described tenor is 50～200 μ g/g；It is preferably
80～150 μ g/g.
And described heterogeneous catalysis is for including lateritic nickel ore, red mud, or fixed bed hydrogenation agent of giving up is a kind of
Or several mixture, addition is the gross weight of described floating bed hydrogenation reactor content
0.1～5.0%；It is preferably 0.5～3.0%.
The method that invention additionally discloses the pyrolysis oil and gas processing combination of a kind of low-order coal, said system, described
Method includes:
Chilling: by out of breath for pyrolysis oil cold, generates cooling oil gas；
Air-distillation: oil gas air-distillation will be cooled down, obtain heavy oil at the bottom of tower and light Fuel；
Cracking, gas-liquid separation: by residual oil cracking at the bottom of tower, gas-liquid separation, obtain cracked oil；
Decompression distillation: residue oil is distilled to obtain in cracked oil decompression；
Residual oil gasification: residue oil gasification is obtained synthesis gas；
Gas separates and purifies: separated by synthesis gas, purify, obtains hydrogen, carbon monoxide；
Ethylene glycol synthesizes: by carbon monoxide and hydrogen synthesizing glycol.
Preferably, described chilling step also generates condensation heavy oil, is sent into by described condensation heavy oil described
Floating bed hydrogenation reactor carries out described cracking.
Or, described decompression distilation steps also generates quench oil, is respectively fed to by described quench oil
Described chilling step, described air-distillation step.
Or, pyrolysis gas is also isolated in described air-distillation, and described pyrolysis gas is admitted to described gas
Separate and depurator carries out described gas separation and purifying step.
Or, described gas-liquid separation step also generates cracked gas, is admitted to by described cracked gas described
Gas separates and depurator carries out described gas separation and purifying step.
Or, the hydrogen that described gas separates and purifying step obtains, part is sent into described suspension bed and is added
Hydrogen reactor.
Or, also include the step of pyrolysis oil gas dedusting before chilling step.In chilling step with often
The step of stable cooling oil gas is also included between pressure distilation steps.
Wherein, described quench oil is the fraction less than 500～560 DEG C that cracked oil obtains through decompression distillation.
Heavy residue oil after deep vacuum distillation of the present invention is not recycled to floating bed hydrogenation reactor, it is to avoid
Coking during floating bed hydrogenation；Residue oil is carried out catalytic gasification, gasification gas and pyrolysis gas through clean
Change the raw material as production ethylene glycol after separating, improve the motility of coal tar heavy component processing,
Improve process economy；It addition, the decompression light fraction part that the present invention uses floating bed hydrogenation product is made
For being pyrolyzed the cooling medium of oil gas, part feeds as atmospheric distillation tower, this cooling medium heat stability
Preferably, it is to avoid the secondary condensation green coke in cooling procedure, avoid water-cooled simultaneously and produce substantial amounts of containing phenol
Sewage, can improve light oil yield；And it is pyrolyzed oil gas advanced person's row quenching, by the heavy in oil gas
Tar cools down, and the tar of relative lightweight and pyrolysis gas enter atmospheric distillation tower, continues separate out light
Matter fraction, can make full use of just cold oil gas heat, it is to avoid redistilled energy consumption after cooling completely；
The isolated hydrogen of pyrolysis gas be used for coal tar heavy ingredients suspension bed hydroprocessing cracking, it is achieved hydrogen from
Give, save hydrogen manufacturing cost.
Accompanying drawing explanation
Fig. 1 is the schematic diagram that the present invention is pyrolyzed oil and gas processing combined system embodiment；
Fig. 2 is the schematic diagram that the present invention is pyrolyzed oil and gas processing combined method embodiment.
Accompanying drawing 2 description of symbols
1, pyrolysis oil gas, 2, cleaner unit, 3, oil gas 4, quencher after dedusting, 5, first cold oil gas,
6, regulator, 8, atmospheric distillation tower, 9, pyrolysis gas, 10, naphtha cut, 11, diesel oil distillate,
12, heavy oil at the bottom of atmospheric tower, 13, condensation heavy oil fraction, 14, catalyst, 15, floating bed hydrogenation anti-
Answer device, 16, floating bed hydrogenation product, 17, gas-liquid separator, 18, cracked gas, 19, cracked oil,
20, vacuum distillation tower, 21,22,23, quench oil, 24, VACUUM TOWER BOTTOM residue oil, 25, residual oil
Gasifier, 26, gasification gas, 27, gas separate and depurator, 28,29, hydrogen, 30, one oxygen
Change carbon, 31, other lower carbon number hydrocarbons, 32, ethylene glycol synthesis technique system, 33, ethylene glycol, 34, its
Its product
Detailed description of the invention
The open a kind of low-order coal pyrolysis oil and gas processing combined system of the present invention and method, will pyrolysis oil gas warp
Chilling, air-distillation, cracking separation, deep vacuum distillation, gained heavy component is not recycled to suspension bed and adds
Hydrogen reactor, it is to avoid the coking during floating bed hydrogenation；Residue oil gasifies, and gained synthesizes
Edema caused by disorder of QI from and purify, isolate carbon monoxide, hydrogen as the raw material of synthesizing glycol, improve heat
Solve the motility of oil gas heavy component processing, improve process economy.
Specifically, the open a kind of low-order coal pyrolysis oil and gas processing combined system of the present invention and method, be profit
With the part light components after the coal tar suspension bed hydrogenation of heavy as pyrolysis oil gas quench oil, part
As the charging of atmospheric distillation tower, heavy tar at the bottom of condensation heavy tar, atmospheric tower adds as suspension bed
The raw material of hydrogen cracking, VACUUM TOWER BOTTOM heavy tar carries out vaporizing system synthesis gas, pyrolysis gas, cracked gas,
Heavy tar gasification synthesis gas through gas separate and purify, isolate carbon monoxide, hydrogen and other
Lower carbon number hydrocarbons, carbon monoxide, hydrogen are as the raw material of synthesizing glycol, and hydrogen partial is suspension bed simultaneously
Hydrogenation reaction provides hydrogen source, and other lower carbon number hydrocarbons is as pyrolysis oven fuel gas.
Low-order coal disclosed by the invention pyrolysis oil and gas processing combined system, system includes: quencher, often
Pressure distillation column, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device,
Gas separates 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 outlet and light Fuel exports；Cooling oil gas entrance
It is connected with the cooling oil gas vent of quencher；Floating bed hydrogenation reactor is provided with heavy oil entrance, hydrogenation produces
Thing exports；Heavy oil entrance connects the heavy oil outlet of atmospheric distillation tower；Gas-liquid separator is provided with hydrogenation products
Entrance and cracked oil outlet；Hydrogenation products entrance connects with the hydrogenation products outlet of floating bed hydrogenation reactor
Connect；Vacuum distillation tower is provided with cracked oil entrance, residue oil outlet；Cracked oil entrance and gas-liquid separator
Cracked oil outlet connect；Residual oil gasification device is provided with residue oil entrance and syngas outlet；Residue oil enters
Mouth exports with the residue oil of vacuum distillation tower and is connected；Gas separate and depurator be provided with synthesis gas entrance,
Hydrogen outlet and carbon monoxide outlet；Synthesis gas entrance connects with the syngas outlet of residual oil gasification device；
Ethylene glycol synthesis system is provided with carbon monoxide inlet and hydrogen inlet；Carbon monoxide inlet separates with gas
And the carbon monoxide outlet of depurator；Hydrogen inlet separates with gas and the hydrogen outlet of depurator
Connect.
Heavy residue oil after deep vacuum distillation of the present invention is not recycled to floating bed hydrogenation reactor, it is to avoid
Coking during floating bed hydrogenation；Residue oil is carried out catalytic gasification, after the gasification purified separation of gas
As the raw material of production ethylene glycol, improve the motility of coal tar heavy component processing, improve technique
Economy.
The present invention is not excluded for recycling the intermediate product of native system, to save the energy, improves efficiency,
As decompression distilled the light components quench oil as quencher of gained, and the pan feeding of air-distillation,
Cyclic process；Chilling gained heavy component is sent into floating bed hydrocracking；Or by air-distillation institute
Obtain pyrolysis gas, the separating obtained cracked gas of hydrogenation products, isolation of purified together with synthesis gas；Isolation of purified
Gained hydrogen sends into suspension bed etc..
Fig. 1 is the schematic diagram that the present invention is pyrolyzed a preferred embodiment of oil and gas processing combined system, please join
According to Fig. 1, the present embodiment low-order coal pyrolysis oil and gas processing combined system includes: cleaner unit 2, quencher 4,
Regulator 6, atmospheric distillation tower 8, floating bed hydrogenation reactor 15, gas-liquid separator 17, decompression are steamed
Evaporate tower 20, residual oil gasification device 25, gas separation and depurator 27 and ethylene glycol synthesis system 32.
Said apparatus connected mode is:
Pyrolysis oven outlet is connected with the entrance of cleaner unit 2.Cleaner unit 2 is by directly from pyrolysis oven out
Pyrolysis coal gas 1 carries out dust removal process, removes the mechanical admixture such as dust in pyrolysis coal gas, obtains dedusting
Rear oil gas 3.
Quencher 4 is provided with pyrolysis oil gas entrance, quench oil entrance, condensation heavy oil outlet and cooling oil gas
Outlet.Pyrolysis oil gas entrance connects the outlet of cleaner unit 2, and after dedusting, oil gas 3 is entered by cleaner unit 2
Quencher 4 carries out chilling operation, 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 regulator 6, by the steady air current of first cold oil gas 5, it is to avoid because of air-flow unstable under
One device causes damage.
Atmospheric distillation tower 8 is provided with cooling oil gas entrance, heavy oil outlet, light Fuel outlet and pyrolysis gas
Outlet.The gas outlet of regulator 6 connects the cooling oil gas entrance of atmospheric distillation tower 8, after stable
Cooling oil gas is sent in atmospheric distillation tower 8 and is reacted, and obtains weight at the bottom of pyrolysis gas 9, light Fuel and tower
Oil 12.The light Fuel that atmospheric distillation tower produces is divided into naphtha cut 10 and diesel oil distillate 11, gently
Matter fuel outlet is divided into naphtha cut outlet and diesel oil distillate to export the most accordingly.
Floating bed hydrogenation reactor 15 is provided with heavy oil entrance, hydrogen inlet and hydrogenation products outlet.Heavy oil
Entrance connects the heavy oil outlet of atmospheric distillation tower 8 and the condensation heavy oil outlet of quencher, hydrogen 28 He
Carry out cracking reaction under the effect of catalyst converter, obtain hydrogenation products 16.
Gas-liquid separator 17 is provided with hydrogenation products entrance, cracking gas exit and cracked oil outlet.Hydrogenation produces
Thing entrance connects the hydrogenation products outlet of floating bed hydrogenation reactor 15, and hydrogenation products 16 enters gas-liquid
The cracked gas 18 of separator 17 separation and cracked oil 19.
Vacuum distillation tower 20 is provided with cracked oil entrance, quench oil outlet and residue oil outlet.Cracked oil enters
The cracked oil outlet of mouth connection gas-liquid separator 17, cracked oil 19 is admitted to vacuum distillation tower 20 to be carried out
Decompression distillation, obtains residue oil 24 and the light components 21 of heavy component.Quench oil outlet connects respectively
The quench oil entrance of quencher 4 and the quench oil entrance of atmospheric distillation tower 8.A part for light components
Being admitted to quencher 4 as quench oil, a part sends into atmospheric distillation tower 8, air-distillation as raw material
The cooling oil gas entrance of tower 8 and quench oil entrance can be same entrance, are feed(raw material)inlet.
Residual oil gasification device 25 is provided with residue oil entrance and syngas outlet.Residue oil entrance connects decompression and steams
Evaporate the residue oil outlet of tower 20.Residue oil 24 is entered residual oil gasification device 25 gas by vacuum distillation tower 20
Change, generate synthesis gas 26.
Gas separates and depurator 27 is provided with synthesis gas entrance, pyrolysis gas entrance, cracked gas entrance, hydrogen
Gas outlet and carbon monoxide outlet and fuel gas export.Synthesis gas entrance connects the conjunction of residual oil gasification device 25
Become gas outlet.Pyrolysis gas entrance connects the pyrolysis gas outlet of atmospheric distillation tower 8.Cracked gas entrance connects
The cracking gas exit of gas-liquid separator 17.The synthesis gas of residual oil gasification device 25 generation, atmospheric distillation tower 8
The pyrolysis gas, the cracked gas of gas-liquid separator 17 generation that produce are admitted to gas and separate and depurator 27,
Separate, obtain 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 export and other
Product exit.Hydrogen inlet, carbon monoxide inlet connect gas respectively and separate and the hydrogen of depurator 27
Outlet, carbon monoxide outlet.Gas separate and depurator 27 produce a part of hydrogen 28 and an oxygen
Change carbon 30 to be admitted in ethylene glycol synthesis system 32 synthesize, obtain ethylene glycol 33 and other product
34。
The hydrogen outlet of gas separation and depurator 27 also connects the hydrogen of floating bed hydrogenation reactor 15
Entrance.
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.
Catalyst used by floating bed hydrogenation reactor of the present invention can be comprise Mo, Ni, Co, W,
Homogeneous or the heterogeneous catalysis of one or more metals in Fe.Homogeneous catalyst include naphthenate,
One or more in soap, metal complex, wherein, measure with metallic element, and metal contains
Amount is 50～200 μ g/g；It is preferably 80～150 μ g/g.
And heterogeneous catalysis can be to include lateritic nickel ore, red mud, or fixed bed hydrogenation agent of giving up is a kind of
Or several mixture, addition is the 0.1～5.0% of the gross weight of floating bed hydrogenation reactor content,
It is preferably 0.5～3.0%.
Residual oil gasification unit of the present invention use part residue oil partial oxidation technology to generate with carbon monoxide and
Hydrogen is main raw material of synthetic gas, and gasifying agent is oxygen and steam, and wherein oxygen oil ratio is 0.4～0.8
(m3/ kg oil).
Gasification reaction is using natural crystal as gasification auxiliary agent, such as dolomite, olivine, clay Ore
One or more, addition is 0.1～2.0% (mass percent of gasifier combined feed), preferably
0.2～1.5%.Gasification temperature 800～1100 DEG C, the response time 0.1～5s, preferably 0.5～3.0s.
Floating bed hydrogenation reaction condition is: temperature 400～485 DEG C, preferably 420～475 DEG C, pressure
10～25Mpa, preferably 12～24Mpa.
Pyrolysis oil gas is cooled to 410～480 DEG C at pyrolysis gas quenching unit, preferably 420～460 DEG C, enters
The cooling oil gas temperature entering atmospheric distillation tower is preferably 380～450 DEG C.
It should be noted that connection of the present invention or connection, refer to pipeline or other equipment,
The product that previous device produces is sent in next device.
The method that invention additionally discloses the pyrolysis oil and gas processing combination of a kind of low-order coal, the method application is above-mentioned
System works, and method comprises the steps:
Chilling: by out of breath for pyrolysis oil cold, generates cooling oil gas；
Air-distillation: oil gas air-distillation will be cooled down, obtain heavy oil at the bottom of tower and light Fuel；
Cracking, gas-liquid separation: by residual oil cracking at the bottom of tower, gas-liquid separation, obtain cracked oil；
Decompression distillation: residue oil is distilled to obtain in cracked oil decompression；
Residual oil gasification: residue oil gasification is obtained synthesis gas；
Gas separates and purifies: separated by synthesis gas, purify, obtains 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 the present invention, makes full use of pyrolysis simultaneously
Oil gas, therefore the method for low-order coal of the present invention pyrolysis oil and gas processing combination can also include following either step,
Or multiple step therein:
Condensation heavy oil chilling step generated is sent into floating bed hydrogenation reactor and is carried out cracking；
The quench oil generated by decompression distilation steps, respectively as quench oil with sending into chilling step, work
Air-distillation is sent into for raw material；
By air-distillation generate pyrolysis gas send into gas separate and depurator carry out described gas separation and
Purify；
By gas-liquid separation step generate cracked gas send into gas separate and depurator carry out gas separation and
Purifying step；
The hydrogen partial that gas separation and purifying step obtain is sent into described floating bed hydrogenation reactor auxiliary
Help cracking reaction；
Especially, the present invention also includes the step of pyrolysis oil gas dedusting before chilling step.Or,
The step of stable cooling oil gas is also included between chilling step and air-distillation step.
Fig. 2 is the schematic diagram that the present invention is pyrolyzed oil and gas processing combined method embodiment, as in figure 2 it is shown,
The method of the present embodiment low-order coal pyrolysis oil and gas processing combination comprises the following steps:
(1) pyrolysis gas chilling list is entered after the mechanical admixtures such as pyrolysis oil gas enters cleaner unit, removing dust
Unit, is pyrolyzed oil gas by the part quench oil Quench from decompression distillation, it is thus achieved that condensation in quenching unit
Heavy oil and first cold oil gas；
(2) just cold oil gas enter behind regulator atmospheric distillation tower fractionate out 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 light components and heavy component, and light components is made
For quench oil, be partly into pyrolysis gas quenching unit, a part as the raw material of atmospheric distillation tower,
Heavy residue oil ingredient enters residual oil gasification unit and 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 as synthesizing glycol raw material, same
Time hydrogen partial be floating bed hydrogenation reaction provide hydrogen source, other lower carbon number hydrocarbons is as pyrolysis oven fuel gas.
The present invention distillation unit that reduces pressure carries out deep vacuum distillation, and light, heavy constituent cut point controls
500～565 DEG C.The light component fraction less than 500～560 DEG C that cracked oil obtains through decompression distillation, one
Being allocated as removing pyrolysis oil gas for quench oil, a part removes distillation column；Can after heavy oil gasification residue treatment
As suspension bed hydrogenation catalyst.
Those skilled in the art can be according to oil product decompression determination of distillation method standard GB/T
9168-1997, controls the parameter of vacuum distillation tower, obtains the above-mentioned cut point of cracked oil, thus control
Cracked oil, the composition of cracked gas.
Describe the present invention in detail with specific embodiment below, but the most therefore embodiment limits this
The range of invention.Detailed description of the invention is according to technological process shown in Fig. 2, and processed Hunchun is low
The oil gas that rank 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
Table 2 Hunchun coal pyrolysis gas composition
Embodiment 1
It is cooled to 420 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 400 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 420 DEG C, pressure 12Mpa, catalyst is molybdenum naphthenate,
Measuring with metallic element, tenor is 80 μ g/g, and vulcanizing agent is Sublimed Sulfur powder, addition 80 μ g/g,
Decompression distillation is light, the cutting temperature of heavy constituent is 520 DEG C, and residue oil gasification auxiliary agent selects dolime,
Addition 0.3%, gasifying agent is steam and oxygen, and oxygen oil ratio is 0.4, gasification temperature 850 DEG C, instead
0.8S between Ying Shi, pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and purification systems, divide
Separating out carbon monoxide, hydrogen and other lower carbon number hydrocarbons, high-purity CO, hydrogen are sent into ethylene glycol and are closed
Architectonical.Primary product index is shown in Table 3.
Embodiment 2
It is cooled to 440 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 420 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 450 DEG C, pressure 18Mpa, add heterogeneous catalysis,
Selecting laterite nickel and the mixture of red mud, addition 0.5%, homogeneous catalyst is tungsten complex,
Measuring with metallic element, tenor is 50 μ g/g, and vulcanizing agent is Sublimed Sulfur powder, addition 100 μ g/g,
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%, gasifying agent is steam and oxygen, and oxygen oil ratio is 0.6, gasification temperature 900 DEG C, instead
1.2S between Ying Shi, pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and purification systems, divide
Separating out carbon monoxide, hydrogen and other lower carbon number hydrocarbons, high-purity CO, hydrogen are sent into ethylene glycol and are closed
Architectonical.Primary product index is shown in Table 3.
Embodiment 3
It is cooled to 460 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 450 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 475 DEG C, pressure 24Mpa, add heterogeneous catalysis solid
The useless agent of fixed bed hydrogenation, addition 3%, vulcanizing agent is Sublimed Sulfur powder, and decompression distillation is light, the cutting of heavy constituent
Cutting temperature is 565 DEG C, and residue oil gasification auxiliary agent selects calcined clay ore deposit, addition 1.5%, gasifying agent
For steam and oxygen, oxygen oil ratio is 0.75, gasification temperature 1000 DEG C, response time 3.0S, pyrolysis
Gas, cracked gas, residual oil gasification gas enter gas and separate and purification systems, isolate carbon monoxide, hydrogen
Gas and other lower carbon number hydrocarbons, high-purity CO, hydrogen send into ethylene glycol synthetic system.Primary product
Index is shown in Table 3.
Embodiment 4
It is cooled to 410 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 380 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 400 DEG C, pressure 10Mpa, catalyst is the alkanoic acid of Mo
Salt, the fatty acid of Co, the compositions of complex of Ni, measure with metallic element, and tenor is
200 μ g/g, vulcanizing agent is Sublimed Sulfur powder, addition 80 μ g/g, and decompression distillation is light, the cutting of heavy constituent
Temperature is 500 DEG C, residue oil gasification auxiliary agent selection dolime and olivine, addition 2.0%,
Gasifying agent is steam and oxygen, and oxygen oil ratio is 0.8, gasification temperature 850 DEG C, response time 0.5S,
Pyrolysis gas, cracked gas, residual oil gasification gas enter gas separate and purification systems, isolate carbon monoxide,
Hydrogen and other lower carbon number hydrocarbons, high-purity CO, hydrogen send into ethylene glycol synthetic system.Main product
Thing index is shown in Table 3.
Embodiment 5
It is cooled to 480 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 430 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 485 DEG C, pressure 25Mpa, catalyst is red mud, adds
The 5.0% of the gross weight that amount is floating bed hydrogenation reactor content.Vulcanizing agent is Sublimed Sulfur powder, addition
80 μ g/g, decompression distillation is light, the cutting temperature of heavy constituent is 520 DEG C, and residue oil gasification auxiliary agent selects to forge
Calcined dolomite, addition 0.3%, gasifying agent is steam and oxygen, and oxygen oil ratio is 0.8, gasification temperature
1100 DEG C, response time 0.1S, pyrolysis gas, cracked gas, residual oil gasification gas enter gas and separate and clean
Change system, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, and high-purity CO, hydrogen send
Enter ethylene glycol synthetic system.Primary product index is shown in Table 3.
Embodiment 6
It is cooled to 480 DEG C at pyrolysis oil gas quenching unit, through steady after pyrolysis oil gas removing dust unit dedusting
Determining to isolate pyrolysis gas with 450 DEG C of entrance atmospheric distillation towers, top after device is stablized, stone brain isolated by side line
Oil distillate, diesel oil distillate, at the bottom of atmospheric tower, heavy oil, first cold heavy oil are as floating bed hydrocracking unit
Charging, slurry-bed hydrocracking temperature 450 DEG C, pressure 20Mpa, catalyst is containing red mud, red
Mud addition is the 0.1% of the gross weight of floating bed hydrogenation reactor content, the soap of W, Fe,
Tenor is 150 μ g/g.Vulcanizing agent is Sublimed Sulfur powder, addition 80 μ g/g, and decompression distillation is light, weight
The cutting temperature of component is 500 DEG C, residue oil gasification auxiliary agent selection dolime, addition 0.1%,
Gasifying agent is steam and oxygen, and oxygen oil ratio is 0.6, gasification temperature 800 DEG C, response time 5S, heat
Vent one's spleen, cracked gas, residual oil gasification gas enter gas separate and purification systems, isolate carbon monoxide,
Hydrogen and other lower carbon number hydrocarbons, high-purity CO, hydrogen send into ethylene glycol synthetic system.Main product
Thing index is shown in Table 3.
Table 3 embodiment primary product is distributed
Low-order coal disclosed by the invention pyrolysis oil and gas processing combined system and method, be to utilize heavy coal tar
Part light components after oil floating bed hydrogenation steams as normal pressure as the quench oil of pyrolysis oil gas, part
Evaporate the charging of tower, former as floating bed hydrocracking of heavy tar at the bottom of condensation heavy tar, atmospheric tower
Material, VACUUM TOWER BOTTOM heavy tar carries out vaporizing system synthesis gas, pyrolysis gas, cracked gas, heavy tar gas
It is combined to gas separate through gas and purify, isolates carbon monoxide, hydrogen and other lower carbon number hydrocarbons, one
Carbonoxide, hydrogen are as synthesizing glycol raw material, and hydrogen partial provides for floating bed hydrogenation reaction simultaneously
Hydrogen source, other lower carbon number hydrocarbons is as pyrolysis oven fuel gas.
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 present invention 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. a low-order coal pyrolysis oil and gas processing combined system, it is characterised in that including: quencher,
Atmospheric distillation tower, floating bed hydrogenation reactor, gas-liquid separator, vacuum distillation tower, residual oil gasification device,
Gas separates and depurator and ethylene glycol synthesis system；
Described quencher is provided with cooling oil gas vent；
Described atmospheric distillation tower is provided with cooling oil gas entrance, heavy oil outlet and light Fuel outlet；Described
Cooling oil gas entrance is connected with the cooling oil gas vent of described quencher；
Described floating bed hydrogenation reactor is provided with heavy oil entrance, hydrogenation products outlet；Described heavy oil entrance
Connect the heavy oil outlet of described atmospheric distillation tower；
Described gas-liquid separator is provided with hydrogenation products entrance and cracked oil outlet；Described hydrogenation products entrance
Export with the hydrogenation products of described floating bed hydrogenation reactor and be connected；
Described vacuum distillation tower is provided with cracked oil entrance, residue oil outlet；Described cracked oil entrance and institute
The cracked oil outlet stating gas-liquid separator connects；
Described residual oil gasification device is provided with residue oil entrance and syngas outlet；Described residue oil entrance and institute
The residue oil outlet stating vacuum distillation tower connects；
Described gas separates and depurator is provided with synthesis gas entrance, hydrogen outlet and carbon monoxide outlet；
Described synthesis gas entrance connects with the syngas outlet of described residual oil gasification device；
Described ethylene glycol synthesis system is provided with carbon monoxide inlet and hydrogen inlet；Described carbon monoxide enters
Mouth separates and the carbon monoxide outlet of depurator with described gas；Described hydrogen inlet and described gas
Body separates and the hydrogen outlet of depurator connects.
2. the system as claimed in claim 1, it is characterised in that described quencher is provided with condensation heavy oil
Outlet, the outlet of described condensation heavy oil is connected with the heavy oil entrance of described floating bed hydrogenation reactor；
Or, described vacuum distillation tower is provided with quench oil outlet, and described quencher is provided with quench oil entrance,
Described atmospheric distillation tower is provided with quench oil entrance, the outlet of described quench oil and the quench oil of described quencher
Entrance, the quench oil entrance of described atmospheric distillation tower connect；
Or, described atmospheric distillation tower is provided with pyrolysis gas outlet, and described gas separates and depurator is provided with
Pyrolysis gas entrance, described pyrolysis gas outlet connects described gas and separates and the pyrolysis gas entrance of depurator；
Or, described gas-liquid separator is provided with cracking gas exit, and described gas separates and depurator is provided with
Cracked gas entrance, described cracking gas exit connects described gas and separates and the cracked gas entrance of depurator；
Or, described floating bed hydrogenation reactor is provided with hydrogen inlet, described floating bed hydrogenation reactor
Hydrogen inlet connect described gas separate and the hydrogen outlet of depurator；
Or, described system farther includes cleaner unit, and the outlet of described cleaner unit connects described chilling
The pyrolysis oil gas entrance of device；
Or, described system farther includes regulator, and the air intake of described regulator connects described urgency
The cooling oil gas vent of cooler, the gas outlet of described regulator connects the cooling oil of described atmospheric distillation tower
Gas entrance.
3. the system as claimed in claim 1, it is characterised in that described floating bed hydrogenation reactor institute
Catalyst be containing one or more metals homogeneous or heterogeneous in Mo, Ni, Co, W, Fe
Catalyst；
Described homogeneous catalyst includes the one in naphthenate, soap, metal complex or several
Kind, wherein, measuring with metallic element, described tenor is 50～200 μ g/g；
Described heterogeneous catalysis is for including lateritic nickel ore, red mud, or fixed bed hydrogenation gives up a kind of in agent
Or several mixture, addition is the gross weight of described floating bed hydrogenation reactor content
0.1～5.0%.
4. system as claimed in claim 3, it is characterised in that described tenor is 80～150 μ g/g.
5. system as claimed in claim 3, it is characterised in that addition is described floating bed hydrogenation
The 0.5～3.0% of the gross weight of reactor content.
6. a low-order coal pyrolysis oil and gas processing combined method, applies described in any one of claim 1-5
System, it is characterised in that described method includes:
Chilling: by out of breath for pyrolysis oil cold, generates cooling oil gas；
Air-distillation: oil gas air-distillation will be cooled down, obtain heavy oil at the bottom of tower and light Fuel；
Cracking, gas-liquid separation: by residual oil cracking at the bottom of tower, gas-liquid separation, obtain cracked oil；
Decompression distillation: residue oil is distilled to obtain in cracked oil decompression；
Residual oil gasification: residue oil gasification is obtained synthesis gas；
Gas separates and purifies: separated by synthesis gas, purify, obtains hydrogen, carbon monoxide；
Ethylene glycol synthesizes: by carbon monoxide and hydrogen synthesizing glycol.
7. method as claimed in claim 6, it is characterised in that described chilling step also generates cold
Dignified oil, carries out described cracking by the described condensation heavy oil described floating bed hydrogenation reactor of feeding；
Or, described decompression distilation steps also generates quench oil, is respectively fed to by described quench oil
Described chilling step, described air-distillation step；
Or, pyrolysis gas is also isolated in described air-distillation, and described pyrolysis gas is admitted to described gas
Separate and depurator carries out described gas separation and purifying step；
Or, described gas-liquid separation step also generates cracked gas, is admitted to by described cracked gas described
Gas separates and depurator carries out described gas separation and purifying step；
Or, the hydrogen that described gas separates and purifying step obtains, part is sent into described suspension bed and is added
Hydrogen reactor.
8. method as claimed in claim 6, it is characterised in that also include heat before chilling step
Solve the step of oil gas dedusting.
9. method as claimed in claim 6, it is characterised in that walk in chilling step and air-distillation
The step of stable cooling oil gas is also included between Zhou.
10. method as claimed in claim 7, it is characterised in that described quench oil is cracked oil warp
The fraction less than 500～560 DEG C that decompression distillation obtains.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610515416.6A CN105936834A (en) | 2016-07-01 | 2016-07-01 | Combined system and method for processing oil gas generated by pyrolysis of low rank coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610515416.6A CN105936834A (en) | 2016-07-01 | 2016-07-01 | Combined system and method for processing oil gas generated by pyrolysis of low rank coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105936834A true CN105936834A (en) | 2016-09-14 |
Family
ID=56873275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610515416.6A Pending CN105936834A (en) | 2016-07-01 | 2016-07-01 | Combined system and method for processing oil gas generated by pyrolysis of low rank coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105936834A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106349766A (en) * | 2016-09-23 | 2017-01-25 | 北京神雾环境能源科技集团股份有限公司 | System and method for producing carbon black from coal tar |
| CN109233890A (en) * | 2018-09-04 | 2019-01-18 | 新奥科技发展有限公司 | A kind of oil gas coproduction gasification process and device |
| CN113046104A (en) * | 2021-03-19 | 2021-06-29 | 重庆大学 | Pyrolysis device and pyrolysis method for red mud catalytic biomass infrared pyrolysis |
| CN114685238A (en) * | 2020-12-25 | 2022-07-01 | 蓝星（北京）技术中心有限公司 | Process and device for continuously producing chloroprene |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311796A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed hydrogenation process method |
| CN205328897U (en) * | 2015-12-30 | 2016-06-22 | 宁波金远东石化工程技术有限公司 | Device of synthetic ethylene glycol |
| CN106051943A (en) * | 2016-07-05 | 2016-10-26 | 广东绿岛风室内空气系统科技有限公司 | Energy-saving air purifier |
-
2016
- 2016-07-01 CN CN201610515416.6A patent/CN105936834A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311796A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed hydrogenation process method |
| CN205328897U (en) * | 2015-12-30 | 2016-06-22 | 宁波金远东石化工程技术有限公司 | Device of synthetic ethylene glycol |
| CN106051943A (en) * | 2016-07-05 | 2016-10-26 | 广东绿岛风室内空气系统科技有限公司 | Energy-saving air purifier |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106349766A (en) * | 2016-09-23 | 2017-01-25 | 北京神雾环境能源科技集团股份有限公司 | System and method for producing carbon black from coal tar |
| CN109233890A (en) * | 2018-09-04 | 2019-01-18 | 新奥科技发展有限公司 | A kind of oil gas coproduction gasification process and device |
| CN114685238A (en) * | 2020-12-25 | 2022-07-01 | 蓝星（北京）技术中心有限公司 | Process and device for continuously producing chloroprene |
| CN113046104A (en) * | 2021-03-19 | 2021-06-29 | 重庆大学 | Pyrolysis device and pyrolysis method for red mud catalytic biomass infrared pyrolysis |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103160294B (en) | Omnibearing coproduction system and method by utilizing coal grading | |
| CN104004547B (en) | Coal gasification and coal coking co-supply and cogeneration system and method | |
| CN103160296B (en) | Pyrolysis gasification coupling integrated poly-generation system and process for coal chemical industry | |
| CN101580728B (en) | Process technology for non-caking coal or weak caking coal | |
| AU2018222933B2 (en) | Combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar | |
| CN104232147B (en) | A kind of heavy oil lightweight treatment technique | |
| CN101845319B (en) | Process for producing wax and clean fuel oil by using biomass as raw material | |
| CN105936834A (en) | Combined system and method for processing oil gas generated by pyrolysis of low rank coal | |
| US20080256852A1 (en) | Integrated process and apparatus for producing coal-based jet fuel, diesel fuel, and distillate fuels | |
| CN109111950B (en) | Method for producing liquid fuel by hydrogenating full-fraction tar | |
| CN102031135A (en) | Comprehensive processing and utilizing method for heavy oil | |
| CN102559226A (en) | Coal pyrolysis system and pyrolysis method | |
| US3732085A (en) | Thermally efficient nonpolluting system for production of substitute natural gas | |
| CN102559310A (en) | Method for preparing natural gas and other hydrocarbons by using coke-oven gas and other industrial exhaust gases to carry out coal hydrogasification | |
| CN106221792A (en) | A kind of anthracene oil hydrogenation method | |
| CN105950227A (en) | Treatment system and method for pyrolyzed oil gas | |
| WO1980000156A1 (en) | Combined coal liquefaction-gasification process | |
| CN206051957U (en) | A kind of processing system of pyrolysis oil gas | |
| CN106147879A (en) | A kind of rapid pyrolysis oil gas processing system and method | |
| CN106635160B (en) | A kind of coal and coal tar mixed hydrogenation system and technique | |
| CN206051943U (en) | A kind of low-order coal is pyrolyzed oil and gas processing combined system | |
| CN105001890B (en) | A kind of coal chemical industry hydropyrolysis technique and system | |
| CN103992811B (en) | Low-rank coal and Sweet natural gas prepare the method and system of liquid fuel and electricity | |
| CN207944067U (en) | The system that biomass coke tar is kneaded made fuel oil with Fischer-Tropsch synthesis oil | |
| US20140296595A1 (en) | Methods And Apparatus For Producing Aromatics From Coal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
|
| CB02 | Change of applicant information | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160914 |
|
| WD01 | Invention patent application deemed withdrawn after publication |