CN106336906A - Low-rank coal treating system and method - Google Patents
Low-rank coal treating system and method Download PDFInfo
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- CN106336906A CN106336906A CN201610899988.9A CN201610899988A CN106336906A CN 106336906 A CN106336906 A CN 106336906A CN 201610899988 A CN201610899988 A CN 201610899988A CN 106336906 A CN106336906 A CN 106336906A
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- 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
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- 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
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
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- Oil, Petroleum & Natural Gas (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a low-rank coal treating system and method. The low-rank coal treating system comprises a pyrolysis unit, a desulfurization and decarburization unit, a sulfur recovery unit, a pyrolysis oil gas treatment unit and a solid residue treatment unit, wherein the pyrolysis unit is used for pyrolysis of low-rank pulverized coal, filtration and cooling of pyrolysis oil gas and separation of an oil-water mixture, the desulfurization and decarburization unit is used for conducting desulfurization and decarburization treatment on gas to obtain product gas, the sulfur recovery unit is used for recovering hydrogen sulfide in the acid gas subjected to desulfurization and decarburization, the hydrogen sulfide is converted into elemental sulfur to serve as a pre-vulcanizing agent of the pyrolysis oil gas treating unit, the pyrolysis oil gas treatment unit is used for reaction of the pre-vulcanizing agent, hydrogen, a catalyst and coal tar, and the solid residue treatment unit is used for treating solid residues and extracted coal to finally obtain ferro-nickel alloy. The low-rank coal treating system can treat the acid gas produced during coal pyrolysis, suspended bed hydrogenation and oil product refining in a unified mode, is cyclically used and achieves harmless and resourceful treatment of outwards thrown solid residues after suspended bed filtration.
Description
Technical field
The invention belongs to coal processing technology field, particularly to a kind of system and method that low-order coal is processed.
Background technology
Coal sub-prime, using the effective way being considered as Coal Clean efficient utilization, is also China " 13 " Coal Chemical Industry
The direction given priority to.The sub-prime of coal using be exactly pass through pyrolysis heterogeneity in coal is first separated, including coal gas,
Tar and semicoke etc..Coal tar can produce gasoline, diesel oil by hydrogenation, and semicoke becomes low volatile, low-sulfur by pyrolysis
Clean fuel, replace dissipating and burn coal and reduce pollution to air.
Using the pyrolytic technique that " leading " is coal, the tar of scale production quantities to be extracted, coal gas, coal sub-prime utilizes coal sub-prime
Need scale, maximization, single set pyrolysis of coal unit scale is more and more large-scale, during the sub-prime of low-order coal utilizes, soon
Speed heat solution typically processes fine coal raw material, and fine coal temperature in pyrolysis oven raises soon, and the time of staying is short, and the coal tar toluene of acquisition is not
Molten thing content is higher, mainly coal ash, coal dust etc., and viscosity larger, containing heavy component is many, heat endurance is poor, belong to heavy,
The category of tar inferior, these shortcomings lead to its deep processing difficulty larger.
Prior art discloses a kind of pyrolysis of coal tar recovery method, this invention is to return pyrolysis gas in tar with cold tar
Receive in tower and carry out contact heat-exchanging, so that the tar condensing in pyrolysis gas is reclaimed, a part of condensed tar is through heat recovery and through solid-liquid
Isolate the cooling medium as pyrolysis gas after dust, a part loops back tar and reclaims tower bottom, improve tar and return in tar
Receive the flow velocity of tower bottom, prevent dust deposit blocking recovery tower.This invention is by the use of heavy tar as cooling medium, part heavy
Tar needs to remove dust through separation of solid and liquid, and the dust in heavy tar is difficult to remove, and obtains a certain amount of oil being difficult by
Mud, and the follow-up deep processing difficulty of heavy tar is larger.Additionally, in the method equipped with filler, this section cold for tar recovery tower upper end
But temperature is low, and pyrolysis gas may carry a small amount of heavy tar here condensation, and long-play can block cooling tower.
Prior art also discloses a kind of method improving pyrolysis of coal low temperature tar quality, and the method is by coalite tar
Or carry out copyrolysis in its bottoms addition feed coal, obtain the preparation method of tar and gaseous hydrocarbon product.Concrete grammar is
Coalite tar or its bottoms are uniformly mixed with feed coal, copyrolysis in common entrance pyrolysis oven, obtained liquid
Product, pyrolysis gas, semicoke, product liquid is oil water mixture, obtains coalite tar after water-oil separating.Low temperature in this invention
The viscosity of coal tar or its bottoms is all larger, and it carries out mixed uniformly mode with feed coal can make coal dust become block or mud
Shape, brings difficulty to material screening, broken etc. process.Additionally, pyrolysis oil gas adopts water-cooled, large amount of sewage can be produced, simultaneously heat
Solution oil gas heat does not have effectively utilizes yet.
Content of the invention
The present invention has coupled the fast pyrogenation of coal, the acid tail gas handling process being pyrolyzed oil vapor treatment and producing during being somebody's turn to do
And floating bed hydrogenation solid slag is processed.Aim to provide a kind of with low order fine coal fast pyrogenation as source, pyrolysis oil gas is efficiently sharp
Rationally recycled with, sour gas and floating bed hydrogenation solid slag integrated treatment coal high-efficiency classified utilization technique.This work
Artistic skill is enough to obtain through refining coal, clean fuel liquid using low-order coal as raw material production high-quality, and can recycle pyrolytic process
And petroleum resources cleans the miscellaneous element such as s, n in processing procedure, and can process produced by floating bed hydrogenation reactor
Solid slag, so that solid slag reaches recycling, accomplishes environmental friendliness, output resource rational utilization.
For achieving the above object, a kind of system that low-order coal is processed of the present invention, including pyrolysis unit, desulfurization and decarburization
Unit, sulphur recovery unit, pyrolysis oil vapor treatment unit and solid slag processing unit；Wherein,
Described pyrolysis unit include low order coal powder entrance, first obtain through refining coal export, second obtain through refining coal export, pyrolysis gas go out
Mouthful and water-oil separating after coal tar oil export, described pyrolysis unit be used for low order coal dust pyrolysis, pyrolysis hydrocarbon filter and cooling with
And the separation of oil water mixture；
Described desulfurization and decarburization unit include pyrolysis gas entrance, gas inlet after oil vapor treatment, desulfurization and decarburization solution inlet,
Sour gas outlet after product gas outlet and desulfurization and decarburization, described desulfurization and decarburization unit is used for for gas carrying out desulfurization and decarburization process
Obtain product gas；
Described sulphur recovery unit includes sour gas entrance after desulfurization and decarburization, sulphur recovery solution inlet and presulfurization agent
Outlet, described sulphur recovery unit is changed into elemental sulfur for the recovery of hydrogen sulfide in sour gas after desulfurization and decarburization, hydrogen sulfide
Presulfurization agent as described pyrolysis oil vapor treatment unit；
Described pyrolysis oil vapor treatment unit includes coal tar oil-in, hydrogen inlet after water-oil separating, catalyst inlet, pre- sulphur
Agent entrance, get rid of outward solid slag outlet, offgas outlet, described pyrolysis oil vapor treatment list after light-end products product exit and oil vapor treatment
Unit is used for presulfurization agent, the reaction of hydrogen, catalyst and coal tar, obtains tail gas after light-end products product and oil vapor treatment, oil
After gas disposal, tail gas enters described desulfurization and decarburization unit and continues with；
Described solid slag processing unit includes second and obtains through refining coal entrance, nickeliferous breeze entrance, gets rid of outward solid slag entrance and ferronickel conjunction
Gold outlet, described solid slag processing unit is used for solid slag and the process obtaining through refining coal, finally obtains dilval.
The outlet of described pyrolysis gas is connected with described pyrolysis gas entrance, coal tar oil export and described after described water-oil separating
After water-oil separating, coal tar oil-in is connected, and after described oil vapor treatment, gas inlet is connected with offgas outlet after described oil vapor treatment,
After described desulfurization and decarburization, sour gas outlet is connected with sour gas entrance after described desulfurization and decarburization, and described presulfurization agent exports institute
State presulfurization agent entrance to be connected, described second obtains through refining coal export obtains through refining coal entrance with described second and be connected, described get rid of solid slag outward and go out
Mouthful and described outward get rid of solid slag entrance and be connected.
Further, described pyrolysis unit is connected with splitter box order by fast pyrogenation stove, separator, cooling tower:
Described fast pyrogenation stove is used for the pyrolysis of low order coal dust；
Described separator is used for being pyrolyzed the separation of gas-liquid and solid impurity in oil gas；
Described used for cooling tower in by filter after pyrolysis oil gas cooled down, obtain pyrolysis gas enter described desulfurization and decarburization
Unit, the oil water mixture obtaining enters described splitter box；
Described splitter box is used for carrying out separating by the oil water mixture after cooling, obtains the coal tar after water-oil separating and enters
Described pyrolysis oil vapor treatment unit.
Specifically, described desulfurization and decarburization unit includes absorption tower and regenerator:
Described absorption tower is used for for the gas from described pyrolysis unit and described pyrolysis oil vapor treatment unit carrying out desulfurization
Decarburizing reaction, the desulfurization and decarburization solution absorbing sour gas enters described regenerator；
Described regenerator carries out regeneration process to the described desulfurization and decarburization solution absorbing sour gas, molten after regeneration
Agent returns to absorption tower and recycles, and regenerator tower overhead gas enters described sulphur recovery unit.
Further, described sulphur recovery unit includes sulfur recovery facility and baker:
Described sulfur recovery facility adopts Complexing Iron sulphur recovery solution, reclaims the hydrogen sulfide in sour gas, hydrogen sulfide
It is changed into elemental sulfur to be discharged by bottom of towe；
The elemental sulfur that described baker is used for discharging bottom of towe is dried, and dried elemental sulfur enters as presulfurization agent
Enter described pyrolysis oil vapor treatment unit.
Further, described pyrolysis oil vapor treatment unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries
Hydrogen production device:
Described suspension bed is used for for presulfurization agent, hydrogen, catalyst and coal tar carrying out pre-hydrotreating, the gas obtaining
Hydrogen production device is carried, the oil product obtaining enters described filter described in being discharged into from tower top；
Described filter is used for being filtered the oil product obtaining after pre-hydrotreating, filters the solids product of generation simultaneously
Enter described solid slag processing unit as outer whipping slag；
Described fixed bed is used for for the oil product from described filter carrying out hydrofinishing and hydrocracking reaction, reacts it
Liquid phase product afterwards enters described gas-liquid separator；
Described gas-liquid separator is used for carrying out separating by reacted liquid phase product, and the liquid phase obtaining is as light-end products
Product, the gas that obtains enter described in carry hydrogen production device；
Described put forward hydrogen production device processing gas after the hydrogen that obtains enter described suspension bed and recycle, the sour gas obtaining
Enter described desulfurization and decarburization unit.
Specifically, described solid slag processing unit is connected with molten separating device order by pelletizer, reduction apparatus:
Described pelletizer is used for getting rid of solid slag outward, obtaining through refining coal and the mixed pelletizing of nickeliferous breeze；
Described reduction apparatus are used for being reduced the pelletizing after pelletizing；
Described molten separating device is used for reduzate is melted office and managed to obtain dilval.
The present invention also provides a kind of method that low-order coal is processed, and comprises the steps:
A. it is pyrolyzed: first low order coal dust is pyrolyzed in described pyrolysis unit, then the pyrolysis obtaining oil gas was carried out
Filter and cooling, obtain pyrolysis gas and oil water mixture, finally carry out separating by described oil water mixture；
B. desulfurization and decarburization: in described desulfurization and decarburization unit, gas is carried out desulfurization and decarburization process and obtain product gas and sour gas
Body；
C. sulphur recovery: sour gas carries out vulcanizing hydrogen retrieval after described sulphur recovery unit is to described desulfurization and decarburization,
Hydrogen sulfide is changed into elemental sulfur as the presulfurization agent of described pyrolysis oil vapor treatment unit；
D. it is pyrolyzed oil vapor treatment: carry out presulfurization agent, hydrogen, catalyst and coal tar in described pyrolysis oil vapor treatment unit
Reaction, obtain tail gas after light-end products product and oil vapor treatment, tail gas after described oil vapor treatment transported to described desulfurization and decarburization
Unit continues with；
E. solid slag is processed: is got rid of outward solid slag in described solid slag processing unit, obtains through refining coal and nickeliferous breeze carries out process and obtains
Dilval.
Further, in described step a, first low order coal dust is placed in described fast pyrogenation stove and is pyrolyzed, be pyrolyzed it
The coal part of obtaining through refining obtaining afterwards is discharged by furnace bottom, and a part transports to described solid slag processing unit；
Obtain after pyrolysis described pyrolysis oil gas transport to described separator to gas-liquid-solid is carried out separate；
Then in described cooling tower, the pyrolysis oil gas after filtering is cooled down, obtain described pyrolysis gas and transport to described taking off
Sulphur decarburization unit, described splitter box transported to by the described oil water mixture obtaining；
Finally in described splitter box, the described oil water mixture after cooling down is carried out separating, obtain the coal tar after water-oil separating
Described pyrolysis oil vapor treatment unit transported to by oil.
By the size controlling of described low order fine coal less than or equal to 3mm, described fast pyrogenation stove controls 500～900
DEG C, the temperature control at described cooling tower bottom is at 70～90 DEG C.
Further, in described step b, first will be from described pyrolysis unit and described pyrolysis oil gas on described absorption tower
The gas of processing unit carries out desulfurization and decarburization reaction, and the product gas after reaction are discharged by tower top, absorbs the de- of sour gas
Sulphur decarbonizing solution transports to described regenerator, then carries out regeneration process in described regenerator to desulfurization and decarburization solution, will regenerate it
Solvent afterwards is transported to absorption tower and is recycled, and regenerator tower overhead gas transports to described sulphur recovery unit.
Further, in described step c, first in described sulphur recovery unit using Complexing Iron sulphur as recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, described hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe, so
In described baker, the elemental sulfur that bottom of towe is discharged is dried afterwards, dried elemental sulfur transports to described heat as presulfurization agent
Solution oil vapor treatment unit.
Specifically, in described step d, first in described suspension bed, presulfurization agent, hydrogen, catalyst and coal tar are carried out
Pre-hydrotreating, by the gas obtaining from tower top discharge transport to described in carry hydrogen production device, the oil product obtaining is transported to described filter and is entered
Row filters, and filters the solids product simultaneously producing as outer whipping slag discharge filter；
Then in described fixed bed, hydrofinishing and hydrocracking reaction are carried out to the oil product after filtering, after reaction
Liquid phase product transports to described gas-liquid separator；
Subsequently reacted liquid phase product is carried out separate in described gas-liquid separator, the liquid phase obtaining is lightweight
Oil product product, the gas obtaining transport to described in carry hydrogen production device；
Last carry hydrogen production device to gas treatment after, the hydrogen obtaining is transported to described suspension bed and recycles, obtain
Sour gas is transported to described desulfurization and decarburization unit and is processed further.
Specifically, the ratio of described presulfurization agent and described catalyst is 1:10～30, and described catalyst accounts for described coal tar
The 1～5% of oil quality, described hydrogen is 800～3000:1 with the volume ratio of described coal tar.
Further, in described step e, got rid of outward solid slag, obtained through refining coal and nickeliferous breeze is mixed by 1:5～20:79～94
Carry out pelletizing after conjunction, the pelletizing after shaping reduction temperature be 900～1400 DEG C at, after the reaction of 40～60min,
Reduzate is carried out with molten office reason again and obtains dilval.
The present invention can sufficiently apply the sour gas in whole technological process, and sour gas returns through complex iron desulphurization solution
The sulphur cake received, needs not move through sulfur melting and processes, and after simple drying, the sulphur cake containing part iron ion carries as presulfurization agent
For the presulfurization of tar floating bed hydrogenation catalysts, further, it is possible to pyrolysis of coal, floating bed hydrogenation, oil refinery are produced
Raw acid tail gas are uniformly processed, and recycle.Additionally, the present invention suspension bed can be filtered after outer to get rid of solid slag innoxious
And recycling treatment, traditional pelletizing can be relied in processing procedure to reduce molten division technique, and contain due to getting rid of outward c in solid slag
Amount is higher, therefore, it is possible to the usage amount of reduction c is greatly lowered, and does not need to add any binding agent in balling process.
The additional aspect of the present invention and advantage will be set forth in part in the description, and partly will become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Brief description
Fig. 1 is that the low-order coal of the present invention utilizes system structure diagram.
Fig. 2 is that the low-order coal of the present invention utilizes process chart.
Specific embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in more details, so that energy
The advantage enough more fully understanding the solution of the present invention and its various aspects.However, specific embodiments described below and enforcement
Example is only descriptive purpose, rather than limitation of the present invention.
The present invention is that fine coal carries out obtaining through refining process by fast pyrogenation stove, and solid product is that product obtains through refining coal, is pyrolyzed oil gas
By cooling, gaseous products enter cleaning system through after the process of electrically trapped tar oil device, produce pure pyrolysis gas and enter downstream
Handling process.Pyrolytic tar carries out just hydrotreating through suspension bed, and light components enter fixed bed deep processing and produce difference
The various distillate fuel oils of cut, floating bed hydrogenation process after the solid slag that filters out of product can with breeze, obtain through refining coal by
Ratio is mixed, through pelletizing and reduction treatment thus producing dilval after mixing.
Low-order coal handling process of the present invention, mainly comprises the steps that
(1) fine coal enters down-flow fluidized bed using ECT pyrolysis oven, and the pyrolysis oil gas removing dust device removing bulky grain mechanical admixture of generation is laggard
Enter chilling tower, in chilling tower, carry out spraying cooling,
(2) pyrolysis gas entrance cleaning system carries out purified treatment, the wherein h of the pyrolysis after process2S and co2Reach product gas
Require, sour gas enters sulphur recovery unit, carries out sulphur recovery process；
(3) coal tar that cooling is reclaimed enters suspended-bed reactor after processed, carries out pre- hydrogenation lighting
Process；
(4) oil product after processing enters after filtration treatment, fixed bed hydrogenation refining reaction and be hydrocracked instead
Answer device, produce the product oil of different fractions；
(5) after proposing hydrogen process, sour gas is directly entered sulphur recovery to the gas after fixed bed hydrogenation is processed
Unit is processed；
(6) the sulphur cake that sulphur recovery unit reclaims returns floating bed hydrogenation device as presulfurization agent after being dried and follows
Ring uses.
(7) solid slag that floating bed hydrogenation product filters all carries out at pelletizing with obtaining through refining coal original ore powder and mixing in proportion therewith afterwards
Reason, the spherical raw material of shaping produces dilval after reduction apparatus are reduced.
As Fig. 2, low-order coal of the present invention includes following unit and process using process, and unit includes: fast
Fast pyrolysis oven, separator, cooling tower, absorption tower, regenerator, sulphur recovery, baker, splitter box, suspension bed, filter, solid
Fixed bed, gas-liquid separator, carry hydrogen, pelletizer, reduction apparatus, molten separating device.Detailed process is as follows:
Low order fine coal is pyrolyzed in down-flow fluidized bed using ECT, and pyrolysis gas mixture is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, passes through
After pyrolysis, low order fine coal is changed into and obtains through refining coal, is discharged as product by fast pyrogenation stove bottom；
Enter cooling tower from the pyrolysis oil gas that fast pyrogenation furnace upper end is discharged after filtering, in cooling tower, be pyrolyzed oil gas
Enter tower from cooling tower lower end, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction to contacting cooling from upper end, not cooled gas
Discharge cooling tower from tower top, the oil water mixture after cooling is flowed out by bottom of towe；
Pyrolysis gas and through carrying hydrogen process after hydrogenation reaction tail gas mixing after by have absorption tower lower end enter, desulfurization
Solvent flows into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction are by tower
Top row goes out, and the desulfuration solution absorbing sour gas enters regenerator；
Absorb the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Use, regenerator tower overhead gas is discharged into next unit；
Regeneration column overhead sour gas enters sulphur recovery unit, and sulphur recovery unit adopts Complexing Iron sulphur recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Enter baker after the elemental sulfur discharged by bottom of towe to be dried, discharge the moisture in the middle of elemental sulfur, single afterwards
Matter sulphur enters floating bed hydrogenation unit as presulfurization agent；
The mixture of the coal tar after the cooling discharged by cooling tower bottom and water enters surge tank, carries out water-oil separating, point
Enter floating bed hydrogenation unit from coal tar afterwards；
Presulfurization agent, hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, the gas after hydrogenation
Body is discharged from suspension bed tower top, and the oil product after pre-hydrotreating enters next unit after filtering；
After filtering, liquid-phase product enters fixed bed hydrogenation unit to the pre- oil product that is hydrogenated with, and filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters and carries hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Get rid of outward solid slag, obtain through refining coal and nickeliferous breeze mix according to a certain percentage this three kinds of materials mixed proportion be 1:5～
20:94～79, carry out pelletizing after mixing, and during this, nickeliferous breeze does not need to carry out any process, and solid due to getting rid of outward
A certain amount of c element is contained, therefore, it is possible to the consumption of obtaining through refining coal as reducing agent is greatly lowered in slag.
Pelletizing after pelletizing is reduced through reduction apparatus, and the metal oxide in pelletizing is in c as reducing agent
Under effect, reduction becomes metal simple-substance, and reduction temperature is 900～1400 DEG C, recovery time 40～60min, and reduzate passes through
Dilval can be produced after the reason of molten office.
The present invention has coupled the fast pyrogenation of coal, the acid tail gas handling process being pyrolyzed oil vapor treatment and producing during being somebody's turn to do
And floating bed hydrogenation solid slag is processed.Can provide a kind of with low order fine coal fast pyrogenation as source, pyrolysis oil gas is efficiently sharp
Rationally recycled with, sour gas and floating bed hydrogenation solid slag integrated treatment coal high-efficiency classified utilization technique.This work
Artistic skill is enough to obtain through refining coal, clean fuel liquid using low-order coal as raw material production high-quality, and can recycle pyrolytic process
And petroleum resources cleans the miscellaneous element such as s, n in processing procedure, and can process produced by floating bed hydrogenation reactor
Solid slag, so that solid slag reaches recycling, accomplishes environmental friendliness, output resource rational utilization.And introducing solid slag to containing
The use of binding agent in balling process can not only be avoided additionally it is possible to utilize the c element that solid slag surface covers in nickel minerals powder, thus
Reduce the consumption of reducing agent c in reduction process.
Below with reference to specific embodiment, present invention is described, it should be noted that these embodiments are only to describe
Property, and limit the present invention never in any form.
Embodiment 1
The present embodiment proposes a kind of system processing coal tar, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery
Unit, pyrolysis oil vapor treatment unit and solid slag processing unit:
Low order fine coal particle diameter (≤3mm), is pyrolyzed in down-flow fluidized bed using ECT, and down-flow fluidized bed using ECT temperature control is 700 DEG C, and pyrolysis oil gas mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
Enter cooling tower from the pyrolysis oil gas that fast pyrogenation furnace upper end is discharged after filtering, in cooling tower, be pyrolyzed oil gas
Enter tower from cooling tower lower end, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction to contacting cooling from upper end, tower after cooling process
At 80 DEG C, not cooled gas discharges cooling tower from tower top to the temperature control at bottom, and the oil water mixture after cooling is by bottom of towe
Flow out；
Pyrolysis gas and through carrying hydrogen process after hydrogenation reaction tail gas mixing after by have absorption tower lower end enter, desulfurization
Solvent flows into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction are by tower
Top row goes out the sulfur content≤20ppm in product gas, co2≤ 2%, the desulfuration solution absorbing sour gas enters regenerator；
Absorb the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Use, regenerator tower overhead gas is discharged into next unit；
Regeneration column overhead sour gas enters sulphur recovery unit, and sulphur recovery unit adopts Complexing Iron sulphur recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Enter baker after the elemental sulfur discharged by bottom of towe to be dried, discharge the moisture in the middle of elemental sulfur, single afterwards
Matter sulphur enters floating bed hydrogenation unit as presulfurization agent, the ratio of presulfurization agent and catalyst for 1:10；
The mixture of the coal tar after the cooling discharged by cooling tower bottom and water enters surge tank, carries out water-oil separating, point
Enter floating bed hydrogenation unit from coal tar afterwards；
Presulfurization agent, hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, and catalyst accounts for tar
The 3% of material quality, hydrogen is 800:1 with the volume ratio of tar.Gas after hydrogenation is discharged from suspension bed tower top, through pre-
Oil product after hydrotreating enters next unit after filtering；
After filtering, liquid-phase product enters fixed bed hydrogenation unit to the pre- oil product that is hydrogenated with, and filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters and carries hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Enter palletizing device outer get rid of solid slag, the ratio of obtaining through refining coal and nickeliferous breeze is 1:15:90, this process mustn't be wanted
Increase any binding agent.
Pelletizing after shaping enters reduction apparatus, and reduction temperature is 900 DEG C, after 50min reduces, enters molten point
Device is processed, and temperature control is at 1350 DEG C.Dilval flows out molten separating device as a solution.
Embodiment 2
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed in down-flow fluidized bed using ECT, and down-flow fluidized bed using ECT temperature control is 800 DEG C, and pyrolysis oil gas mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
Enter cooling tower from the pyrolysis oil gas that fast pyrogenation furnace upper end is discharged after filtering, in cooling tower, be pyrolyzed oil gas
Enter tower from cooling tower lower end, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction to contacting cooling from upper end, tower after cooling process
At 90 DEG C, not cooled gas discharges cooling tower from tower top to the temperature control at bottom, and the oil water mixture after cooling is by bottom of towe
Flow out；
Pyrolysis gas and through carrying hydrogen process after hydrogenation reaction tail gas mixing after by have absorption tower lower end enter, desulfurization
Solvent flows into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction are by tower
Top row goes out the sulfur content≤20ppm in product gas, co2≤ 2%, the desulfuration solution absorbing sour gas enters regenerator；
Absorb the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Use, regenerator tower overhead gas is discharged into next unit；
Regeneration column overhead sour gas enters sulphur recovery unit, and sulphur recovery unit adopts Complexing Iron sulphur recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Enter baker after the elemental sulfur discharged by bottom of towe to be dried, discharge the moisture in the middle of elemental sulfur, single afterwards
Matter sulphur enters floating bed hydrogenation unit as presulfurization agent, the ratio of presulfurization agent and catalyst for 1:20；
The mixture of the coal tar after the cooling discharged by cooling tower bottom and water enters surge tank, carries out water-oil separating, point
Enter floating bed hydrogenation unit from coal tar afterwards；
Presulfurization agent, hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, and catalyst accounts for tar
The 1% of material quality, hydrogen is 1500:1 with the volume ratio of tar.Gas after hydrogenation is discharged from suspension bed tower top, passes through
Oil product after pre-hydrotreating enters next unit after filtering；
After filtering, liquid-phase product enters fixed bed hydrogenation unit to the pre- oil product that is hydrogenated with, and filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters and carries hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Enter palletizing device outer get rid of solid slag, the ratio of obtaining through refining coal and nickeliferous breeze is 1:20:85, this process mustn't be wanted
Increase any binding agent.
Pelletizing after shaping enters reduction apparatus, and reduction temperature is 1200 DEG C, after 40min reduces, enters molten
Separating device is processed, and temperature control is at 1300 DEG C.Dilval flows out molten separating device as a solution.
Embodiment 3
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed in down-flow fluidized bed using ECT, and down-flow fluidized bed using ECT temperature control is 900 DEG C, and pyrolysis oil gas mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
Enter cooling tower from the pyrolysis oil gas that fast pyrogenation furnace upper end is discharged after filtering, in cooling tower, be pyrolyzed oil gas
Enter tower from cooling tower lower end, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction to contacting cooling from upper end, tower after cooling process
At 70 DEG C, not cooled gas discharges cooling tower from tower top to the temperature control at bottom, and the oil water mixture after cooling is by bottom of towe
Flow out；
Pyrolysis gas and through carrying hydrogen process after hydrogenation reaction tail gas mixing after by have absorption tower lower end enter, desulfurization
Solvent flows into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction are by tower
Top row goes out the sulfur content≤20ppm in product gas, co2≤ 2%, the desulfuration solution absorbing sour gas enters regenerator；
Absorb the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Use, regenerator tower overhead gas is discharged into next unit；
Regeneration column overhead sour gas enters sulphur recovery unit, and sulphur recovery unit adopts Complexing Iron sulphur recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Enter baker after the elemental sulfur discharged by bottom of towe to be dried, discharge the moisture in the middle of elemental sulfur, single afterwards
Matter sulphur enters floating bed hydrogenation unit as presulfurization agent, the ratio of presulfurization agent and catalyst for 1:30；
The mixture of the coal tar after the cooling discharged by cooling tower bottom and water enters surge tank, carries out water-oil separating, point
Enter floating bed hydrogenation unit from coal tar afterwards；
Presulfurization agent, hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, and catalyst accounts for tar
The 5% of material quality, hydrogen is 2000:1 with the volume ratio of tar.Gas after hydrogenation is discharged from suspension bed tower top, passes through
Oil product after pre-hydrotreating enters next unit after filtering；
After filtering, liquid-phase product enters fixed bed hydrogenation unit to the pre- oil product that is hydrogenated with, and filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters and carries hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Enter palletizing device outer get rid of solid slag, the ratio of obtaining through refining coal and nickeliferous breeze is 1:5:79, this process mustn't be wanted
Increase any binding agent.
Pelletizing after shaping enters reduction apparatus, and reduction temperature is 1400 DEG C, after 40min reduces, enters molten
Separating device is processed, and temperature control is at 1250 DEG C.Dilval flows out molten separating device as a solution.
Embodiment 4
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed in down-flow fluidized bed using ECT, and down-flow fluidized bed using ECT temperature control is 500 DEG C, and pyrolysis oil gas mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
Enter cooling tower from the pyrolysis oil gas that fast pyrogenation furnace upper end is discharged after filtering, in cooling tower, be pyrolyzed oil gas
Enter tower from cooling tower lower end, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction to contacting cooling from upper end, tower after cooling process
At 80 DEG C, not cooled gas discharges cooling tower from tower top to the temperature control at bottom, and the oil water mixture after cooling is by bottom of towe
Flow out；
Pyrolysis gas and through carrying hydrogen process after hydrogenation reaction tail gas mixing after by have absorption tower lower end enter, desulfurization
Solvent flows into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction are by tower
Top row goes out the sulfur content≤20ppm in product gas, co2≤ 2%, the desulfuration solution absorbing sour gas enters regenerator；
Absorb the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Use, regenerator tower overhead gas is discharged into next unit；
Regeneration column overhead sour gas enters sulphur recovery unit, and sulphur recovery unit adopts Complexing Iron sulphur recovery solution,
Reclaim the hydrogen sulfide in sour gas using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Enter baker after the elemental sulfur discharged by bottom of towe to be dried, discharge the moisture in the middle of elemental sulfur, single afterwards
Matter sulphur enters floating bed hydrogenation unit as presulfurization agent, the ratio of presulfurization agent and catalyst for 1:20；
The mixture of the coal tar after the cooling discharged by cooling tower bottom and water enters surge tank, carries out water-oil separating, point
Enter floating bed hydrogenation unit from coal tar afterwards；
Presulfurization agent, hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, and catalyst accounts for tar
The 3% of material quality, hydrogen is 3000:1 with the volume ratio of tar.Gas after hydrogenation is discharged from suspension bed tower top, passes through
Oil product after pre-hydrotreating enters next unit after filtering；
After filtering, liquid-phase product enters fixed bed hydrogenation unit to the pre- oil product that is hydrogenated with, and filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters and carries hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Enter palletizing device outer get rid of solid slag, the ratio of obtaining through refining coal and nickeliferous breeze is 1:10:94, this process mustn't be wanted
Increase any binding agent.
Pelletizing after shaping enters reduction apparatus, and reduction temperature is 1000 DEG C, after 60min reduces, enters molten
Separating device is processed, and temperature control is at 1450 DEG C.Dilval flows out molten separating device as a solution.
Although embodiments of the invention have been shown and described above it is to be understood that above-described embodiment is example
Property it is impossible to be interpreted as limitation of the present invention, those of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changes, replacing and modification.
What present disclosure was touched upon is exemplary embodiment, in the protection domain defining without departing from claims
In the case of, each embodiment of the application can be made various changes and modifications.Therefore, described embodiment is intended to contain
Cover all such changes, modifications in the protection domain of appended claims and deformation.Additionally, institute unless the context
Refer to outer, the word occurring in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then any embodiment
All or part of can in conjunction with any other embodiment all or part of use.
Claims (10)
1. a kind of system that low-order coal is processed, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery unit, pyrolysis
Oil vapor treatment unit and solid slag processing unit；Wherein,
Described pyrolysis unit include low order coal powder entrance, first obtain through refining coal export, second obtain through refining coal export, pyrolysis gas outlet and
Coal tar oil export after water-oil separating, described pyrolysis unit is used for pyrolysis, pyrolysis hydrocarbon filter and cooling and the oil of low order coal dust
The separation of aqueous mixtures；
Described desulfurization and decarburization unit includes pyrolysis gas entrance, gas inlet, desulfurization and decarburization solution inlet, product after oil vapor treatment
Sour gas outlet after gas outlet and desulfurization and decarburization, described desulfurization and decarburization unit obtains for gas is carried out desulfurization and decarburization process
Product gas；
Sour gas entrance, sulphur recovery solution inlet and presulfurization agent after described sulphur recovery unit includes desulfurization and decarburization goes out
Mouthful, described sulphur recovery unit is changed into elemental sulfur and makees for the recovery of hydrogen sulfide in sour gas after desulfurization and decarburization, hydrogen sulfide
Presulfurization agent for described pyrolysis oil vapor treatment unit；
Described pyrolysis oil vapor treatment unit includes coal tar oil-in, hydrogen inlet after water-oil separating, catalyst inlet, presulfurization agent
Entrance, get rid of outward solid slag outlet, offgas outlet after light-end products product exit and oil vapor treatment, described pyrolysis oil vapor treatment unit is used
In the reaction of presulfurization agent, hydrogen, catalyst and coal tar, obtain tail gas after light-end products product and oil vapor treatment, at oil gas
After reason, tail gas enters described desulfurization and decarburization unit and continues with；
Described solid slag processing unit includes second obtaining through refining coal entrance, nickeliferous breeze entrance, get rid of outward solid slag entrance and dilval goes out
Mouthful, described solid slag processing unit is used for solid slag and the process obtaining through refining coal, finally obtains dilval.
Described pyrolysis gas outlet is connected with described pyrolysis gas entrance, coal tar oil export and described profit after described water-oil separating
After separating, coal tar oil-in is connected, and after described oil vapor treatment, gas inlet is connected with offgas outlet after described oil vapor treatment, described
After desulfurization and decarburization, sour gas outlet is connected with sour gas entrance after described desulfurization and decarburization, and described presulfurization agent outlet is described pre-
Vulcanizing agent entrance is connected, and described second obtains through refining coal export obtains through refining coal entrance with described second and be connected, described outer get rid of solid slag outlet with
The described outer solid slag entrance that gets rid of is connected.
2. system according to claim 1 it is characterised in that
Described pyrolysis unit is connected with splitter box order by fast pyrogenation stove, separator, cooling tower:
Described fast pyrogenation stove is used for the pyrolysis of low order coal dust；
Described separator is used for being pyrolyzed the separation of gas-liquid and solid impurity in oil gas；
Described used for cooling tower in by filter after pyrolysis oil gas cooled down, obtain pyrolysis gas enter described desulfurization and decarburization list
Unit, the oil water mixture obtaining enters described splitter box；
Described splitter box is used for carrying out separating by the oil water mixture after cooling, obtains the entrance of the coal tar after water-oil separating described
Pyrolysis oil vapor treatment unit.
3. system according to claim 1 it is characterised in that
Described desulfurization and decarburization unit includes absorption tower and regenerator:
Described absorption tower is used for for the gas from described pyrolysis unit and described pyrolysis oil vapor treatment unit carrying out desulfurization and decarburization
Reaction, the desulfurization and decarburization solution absorbing sour gas enters described regenerator；
Described regenerator carries out regeneration process to the described desulfurization and decarburization solution absorbing sour gas, and the solvent after regeneration returns
Go back to absorption tower to recycle, regenerator tower overhead gas enters described sulphur recovery unit；
Described sulphur recovery unit includes sulfur recovery facility and baker:
Described sulfur recovery facility adopts Complexing Iron sulphur recovery solution, reclaims the hydrogen sulfide in sour gas, and hydrogen sulfide changes
Discharged by bottom of towe for elemental sulfur；
The elemental sulfur that described baker is used for discharging bottom of towe is dried, and dried elemental sulfur enters institute as presulfurization agent
State pyrolysis oil vapor treatment unit.
4. system according to claim 1 it is characterised in that
Described pyrolysis oil vapor treatment unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries hydrogen production device:
Described suspension bed is used for for presulfurization agent, hydrogen, catalyst and coal tar carrying out pre-hydrotreating, and the gas obtaining is from tower
Top carries hydrogen production device described in being discharged into, and the oil product obtaining enters described filter；
Described filter is used for being filtered the oil product obtaining after pre-hydrotreating, filters the solids product conduct of generation simultaneously
Outer whipping slag enters described solid slag processing unit；
Described fixed bed is used for the oil product from described filter being carried out hydrofinishing and hydrocracking reaction, after reaction
Liquid phase product enters described gas-liquid separator；
Described gas-liquid separator is used for carrying out separating by reacted liquid phase product, and the liquid phase obtaining is produced as light-end products
Thing, the gas that obtains enter described in carry hydrogen production device；
Described put forward hydrogen production device processing gas after the hydrogen that obtains enter described suspension bed and recycle, the sour gas obtaining enters
Described desulfurization and decarburization unit.
5. system according to claim 1 it is characterised in that
Described solid slag processing unit is connected with molten separating device order by pelletizer, reduction apparatus:
Described pelletizer is used for getting rid of solid slag outward, obtaining through refining coal and the mixed pelletizing of nickeliferous breeze；
Described reduction apparatus are used for being reduced the pelletizing after pelletizing；
Described molten separating device is used for reduzate is melted office and managed to obtain dilval.
6. a kind of method low-order coal being processed with system described in claim 1 is it is characterised in that include step:
A. be pyrolyzed: first low order coal dust is pyrolyzed in described pyrolysis unit, then by the pyrolysis obtaining oil gas carry out filter and
Cooling, obtains pyrolysis gas and oil water mixture, finally carries out separating by described oil water mixture；
B. desulfurization and decarburization: in described desulfurization and decarburization unit, gas is carried out desulfurization and decarburization process and obtain product gas and sour gas；
C. sulphur recovery: sour gas carries out vulcanizing hydrogen retrieval, sulfuration after described sulphur recovery unit is to described desulfurization and decarburization
Hydrogen is changed into elemental sulfur as the presulfurization agent of described pyrolysis oil vapor treatment unit；
D. it is pyrolyzed oil vapor treatment: carry out the anti-of presulfurization agent, hydrogen, catalyst and coal tar in described pyrolysis oil vapor treatment unit
Should, obtain tail gas after light-end products product and oil vapor treatment, tail gas after described oil vapor treatment is transported to described desulfurization and decarburization unit
Continue with；
E. solid slag is processed: is got rid of outward solid slag in described solid slag processing unit, obtains through refining coal and nickeliferous breeze carries out process and obtains ferronickel
Alloy.
7. method according to claim 6 it is characterised in that
In described step a, first low order coal dust is placed in described fast pyrogenation stove and is pyrolyzed, obtain after pyrolysis obtains through refining coal
A part is discharged by furnace bottom, and a part transports to described solid slag processing unit；
Obtain after pyrolysis described pyrolysis oil gas transport to described separator to gas-liquid-solid is carried out separate；
Then described cooling tower by filter after pyrolysis oil gas cooled down, obtain described pyrolysis gas transport to described desulfurization take off
Carbon unit, described splitter box transported to by the described oil water mixture obtaining；
Finally in described splitter box, the described oil water mixture after cooling down is carried out separating, obtain the coal tar after water-oil separating defeated
To described pyrolysis oil vapor treatment unit；
By the size controlling of described low order fine coal less than or equal to 3mm, described fast pyrogenation stove controls at 500～900 DEG C, institute
The temperature control stating cooling tower bottom is at 70～90 DEG C.
8. method according to claim 6 it is characterised in that
In described step b, first on described absorption tower by the gas from described pyrolysis unit and described pyrolysis oil vapor treatment unit
Body carries out desulfurization and decarburization reaction, and the product gas after reaction are discharged by tower top, and the desulfurization and decarburization solution absorbing sour gas is defeated
To described regenerator, then in described regenerator, regeneration process is carried out to desulfurization and decarburization solution, the solvent after regeneration is transported to
Absorption tower recycles, and regenerator tower overhead gas transports to described sulphur recovery unit；
In described step c, first in described sulphur recovery unit using Complexing Iron sulphur as reclaiming solution, reclaimed using self-loopa
Technique reclaims the hydrogen sulfide in sour gas, and described hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe, then in described baker
The elemental sulfur that bottom of towe is discharged is dried, and dried elemental sulfur transports to described pyrolysis oil vapor treatment list as presulfurization agent
Unit.
9. method according to claim 6 it is characterised in that
In described step d, first in described suspension bed, presulfurization agent, hydrogen, catalyst and coal tar are carried out pre-hydrotreating,
Hydrogen production device is carried, the oil product obtaining is transported to described filter and filtered, and filters described in the gas obtaining is discharged and transported to from tower top
The solids product simultaneously producing is as outer whipping slag discharge filter；
Then in described fixed bed, hydrofinishing and hydrocracking reaction are carried out to the oil product after filtering, by the gas-liquid after reaction
Phase product transports to described gas-liquid separator；
Subsequently reacted liquid phase product is carried out separate in described gas-liquid separator, the liquid phase obtaining is light-end products
Product, the gas obtaining transport to described in carry hydrogen production device；
Last carry hydrogen production device to gas treatment after, the hydrogen obtaining is transported to described suspension bed and recycles, the acidity obtaining
Gas is transported to described desulfurization and decarburization unit and is processed further；
The ratio of described presulfurization agent and described catalyst be 1:10～30, described catalyst account for described coal tar oil quality 1～
5%, described hydrogen is 800～3000:1 with the volume ratio of described coal tar.
10. method according to claim 6 it is characterised in that
In described step e, got rid of outward solid slag, obtain through refining after coal and nickeliferous breeze are mixed by 1:5～20:79～94 and made
Ball, the pelletizing after shaping reduction temperature be 900～1400 DEG C at, after the reaction of 40～60min, then to reduzate
Carry out molten office reason and obtain dilval.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109233908A (en) * | 2018-09-20 | 2019-01-18 | 新奥科技发展有限公司 | A kind of coal catalytic hydrogenation gasification process and device |
| CN114437851A (en) * | 2022-01-29 | 2022-05-06 | 北京旭阳科技有限公司 | Method for quality improvement and desulfurization of high-sulfur fertilizer coal |
| CN114479897A (en) * | 2020-11-13 | 2022-05-13 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar and method and device for preparing fuel oil from coal |
-
2016
- 2016-10-14 CN CN201610899988.9A patent/CN106336906A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109233908A (en) * | 2018-09-20 | 2019-01-18 | 新奥科技发展有限公司 | A kind of coal catalytic hydrogenation gasification process and device |
| CN114479897A (en) * | 2020-11-13 | 2022-05-13 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar and method and device for preparing fuel oil from coal |
| CN114479897B (en) * | 2020-11-13 | 2023-05-26 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar, method and device for producing fuel oil by coal |
| CN114437851A (en) * | 2022-01-29 | 2022-05-06 | 北京旭阳科技有限公司 | Method for quality improvement and desulfurization of high-sulfur fertilizer coal |
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