CN206279155U - A kind of system of utilization low-order coal - Google Patents
A kind of system of utilization low-order coal Download PDFInfo
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- CN206279155U CN206279155U CN201621126092.9U CN201621126092U CN206279155U CN 206279155 U CN206279155 U CN 206279155U CN 201621126092 U CN201621126092 U CN 201621126092U CN 206279155 U CN206279155 U CN 206279155U
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Abstract
The utility model discloses a kind of system of utilization low-order coal, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery unit, catalyst preparation unit and pyrolysis oil vapor treatment unit：Wherein, pyrolysis unit is used for the pyrolysis of low order coal dust, pyrolysis hydrocarbon filter and cooling and the separation of oil water mixture；Desulfurization and decarburization unit obtains product gas for gas to be carried out into desulfurization and decarburization treatment；Sulphur recovery unit is used for after desulfurization and decarburization the recovery of hydrogen sulfide in sour gas, and hydrogen sulfide is further transformed to elemental sulfur；Sour gas is adsorbed with desulfuration adsorbent in catalyst preparation unit, the adsorbent after adsorption saturation is used as the catalyst of the pyrolysis oil vapor treatment unit；Pyrolysis oil vapor treatment unit is used for the reaction of hydrogen, catalyst and coal tar.The utility model can make full use of the sour gas that pyrolysis of coal process and hydrogenation of tar process are produced, and complete the preparation of coal tar suspension bed hydrogenation pretreatment catalyst while sour gas is processed by adsorbent.
Description
Technical field
The utility model belongs to coal processing technology field, more particularly to a kind of system of utilization low-order coal.
Background technology
Coal sub-prime, using being considered as the efficient effective way for utilizing of Coal Clean, is also China " 13 " Coal Chemical Industry
The direction given priority to.It is exactly first to be separated heterogeneity in coal by pyrolysis that the sub-prime of coal is utilized, 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, burn coal and reduce pollution to air instead of dissipating.
Coal sub-prime utilizes the pyrolytic technique that " tap " is coal, to extract tar, the coal gas of scale production quantities, and coal sub-prime is utilized
Scale, maximization are needed, single set pyrolysis of coal unit scale is more and more large-scale, during the sub-prime of low-order coal is utilized, soon
Speed heat solution typically processes fine coal raw material, and fine coal temperature in pyrolysis oven is raised soon, and the residence time is short, and the coal tar toluene of acquisition is not
Molten thing content is higher, mainly coal ash, coal dust etc., and viscosity it is larger, containing heavy component is more, heat endurance is poor, belong to heavy,
The category of tar inferior, these shortcomings cause its deep processing difficulty larger.
Prior art discloses a kind of pyrolysis of coal tar recovery method, the invention is to return pyrolysis gas in tar with cold tar
Contact heat-exchanging is carried out in receipts tower, the tar condensing in pyrolysis gas is reclaimed, a part of condensed tar is through heat recovery and through solid-liquid
The cooling medium as pyrolysis gas after dust is isolated, a part loops back tar and reclaims tower bottom, improve tar and returned in tar
The flow velocity of tower bottom is received, prevents dust deposit from blocking recovery tower.The 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, tar recovery tower upper end is equipped with filler in the method, this section cold
But temperature is low, and pyrolysis gas may carry a small amount of heavy tar and condense herein, and long-play can block cooling tower.
Prior art also discloses a kind of method for improving pyrolysis of coal low temperature tar quality, and the method is by coalite tar
Or copyrolysis are carried out in its bottoms addition feed coal, obtain the preparation method of tar and gaseous hydrocarbon product.Specific method is
Coalite tar or its bottoms are uniformly mixed with feed coal, it is common to enter copyrolysis in pyrolysis oven, obtain liquid
Product, pyrolysis gas, semicoke, product liquid are oil water mixture, and coalite tar is obtained after water-oil separating.It is low in the inventing type
The viscosity of warm coal tar or its bottoms is all larger, its carry out with feed coal mixed uniformly mode coal dust can be made into block or
Pureed, difficulty is brought to the treatment such as material screening, broken.Additionally, pyrolysis oil gas uses water-cooled, large amount of sewage can be produced, while
Pyrolysis oil gas heat is not also utilized effectively.
Utility model content
The utility model has coupled the fast pyrogenation of coal, has been pyrolyzed oil vapor treatment and the acid tail gas treatment produced during this
Technique.Aim to provide a kind of with low order fine coal fast pyrogenation as source, pyrolysis oil gas is efficiently utilized and sour gas is reasonable
The coal high-efficiency classified utilization technique of recycling.The technique can obtain through refining coal using low-order coal as raw material production high-quality, clearly
Clean liquid fuel, and the miscellaneous elements such as S, N that pyrolytic process and petroleum resources are cleaned in processing procedure can be recycled, do
To environment-friendly, output resource rational utilization.
To achieve the above object, the utility model proposes a kind of system of utilization low-order coal, including pyrolysis unit, desulfurization
Decarburization unit, sulphur recovery unit, catalyst preparation unit and pyrolysis oil vapor treatment unit；Wherein,
The pyrolysis unit includes low order coal powder entrance, obtains through refining coal export, the outlet of the first pyrolysis gas, the second pyrolysis gas
Coal tar oil export after outlet and water-oil separating, the pyrolysis unit is used for the pyrolysis of low order coal dust, pyrolysis hydrocarbon filter and cooling
And the separation of oil water mixture；
The desulfurization and decarburization unit includes gas inlet, desulfurization and decarburization solution after the first pyrolysis gas entrance, oil vapor treatment
Entrance, the first product gas outlet and sour gas outlet after desulfurization and decarburization, the desulfurization and decarburization unit are used to enter sour gas
The treatment of row desulfurization and decarburization obtains product gas；
The sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet, the sulphur after desulfurization and decarburization
Recovery unit is used for after desulfurization and decarburization the recovery of hydrogen sulfide in sour gas, and hydrogen sulfide is further transformed to elemental sulfur；
The catalyst preparation unit includes the second pyrolysis gas entrance, the second product gas outlet and catalyst outlet,
The catalyst preparation unit is adsorbed with desulfuration adsorbent to sour gas, and the adsorbent after adsorption saturation is used as the heat
Solve the catalyst of oil vapor treatment unit；
The pyrolysis oil vapor treatment unit includes coal tar oil-in, hydrogen inlet, catalyst inlet, lightweight after water-oil separating
Offgas outlet after oil product product exit and oil vapor treatment, the pyrolysis oil vapor treatment unit is used for hydrogen, catalyst and coal tar
Reaction, obtain tail gas after light-end products product and oil vapor treatment, after oil vapor treatment tail gas enter the desulfurization and decarburization unit after
Continuous treatment；
First pyrolysis gas outlet is connected with the first pyrolysis gas entrance, second pyrolysis gas export with
The second pyrolysis gas entrance is connected, coal tar oil-in phase after coal tar oil export and the water-oil separating after the water-oil separating
Even, gas inlet is connected with offgas outlet after the oil vapor treatment after the oil vapor treatment, sour gas after the desulfurization and decarburization
Outlet is connected with sour gas entrance after the desulfurization and decarburization, and catalyst outlet described in the catalyst inlet is connected.
Specifically, the pyrolysis unit is connected by fast pyrogenation stove, separator, cooling tower with splitter box order：
The fast pyrogenation stove is used for the pyrolysis of low order coal dust；
The separator is used to be pyrolyzed the separation of gas phase liquid phase and solid phase in oil gas；
The pyrolysis oil gas after by filtering used for cooling tower is cooled down, and obtains pyrolysis gas into the desulfurization and decarburization
Unit, the oil water mixture for obtaining enters the splitter box；
The splitter box is used to be separated the oil water mixture after cooling, obtains the entrance of the coal tar after water-oil separating
The pyrolysis oil vapor treatment unit.
Further, the desulfurization and decarburization unit includes absorption tower and regenerator：
The absorption tower is used to for the gas from the pyrolysis unit and the pyrolysis oil vapor treatment unit to carry out desulfurization
Decarburizing reaction, the desulfurization and decarburization solution for absorbing sour gas enters the regenerator；
The regenerator carries out regeneration treatment to the desulfurization and decarburization solution for absorbing sour gas, molten after regeneration
Agent returns to absorption tower and recycles, and regenerator tower overhead gas enters the sulphur recovery unit.
Further, the sulphur recovery unit includes sulfur recovery facility and baker：
The sulfur recovery facility uses 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 baker is used to be dried the elemental sulfur that bottom of towe is discharged.
Specifically, the catalyst preparation unit includes adsorption tower and pulverizer：
The adsorption tower with iron oxide as adsorbent, for being inhaled to the sour gas for coming from the pyrolysis unit
It is attached；
The pulverizer is used to crush the adsorbent after adsorption saturation, enters described as catalyst after crushing
Pyrolysis oil vapor treatment unit.
Further, the pyrolysis oil vapor treatment unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries
Hydrogen production device：
The suspension bed is used to for hydrogen, catalyst and coal tar to carry out pre-hydrotreating, and the gas for obtaining is arranged from tower top
Go out and carry hydrogen production device described in entering, the oil product for obtaining enters the filter；
The filter is used to be filtered the oil product obtained after pre-hydrotreating, while filtering the solids product for producing
As outer whipping slag discharge filter；
The fixed bed is used to for the oil product from the filter to carry out hydrofinishing and hydrocracking reaction, reacts it
Liquid phase product afterwards enters the gas-liquid separator；
The gas-liquid separator is used to be separated reacted liquid phase product, and the liquid phase for obtaining is used as light-end products
Product, the gas for obtaining carries hydrogen production device described in；
The hydrogen obtained after hydrogen production device processing gas that carries is recycled into the suspension bed, the sour gas for obtaining
Into the desulfurization and decarburization unit.
The utility model can make full use of the sour gas that pyrolysis of coal process and hydrogenation of tar process are produced, and by inhaling
The attached dose of preparation that coal tar suspension bed hydrogenation pretreatment catalyst is completed while sour gas is processed.Additionally, this practicality
It is new acid tail gas produced by pyrolysis of coal, floating bed hydrogenation, oil refinery to be uniformly processed, recycle.
Additional aspect of the present utility model and advantage will be set forth in part in the description, partly by from following description
In become obvious, or by it is of the present utility model practice recognize.
Brief description of the drawings
Fig. 1 is that low-order coal of the present utility model utilizes system structure diagram.
Fig. 2 is that low-order coal of the present utility model utilizes process chart.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the present utility model is described in more details, with
Just better understood when the advantage of scheme of the present utility model and its various aspects.However, specific implementations described below side
Formula and embodiment are only descriptive purposes, rather than to limitation of the present utility model.
The utility model is that fine coal carries out obtaining through refining treatment by fast pyrogenation stove, and solid product is that product obtains through refining coal, pyrolysis
By cooling, gaseous products enter cleaning system to oil gas after being processed through electrically trapped tar oil device, produce pure pyrolysis gas and enter
Downstream processes.Pyrolytic tar carries out just hydrotreating by suspension bed, and light components are produced into fixed bed deep processing
The various distillate fuel oils of different fractions.
Low-order coal handling process described in the utility model, mainly includes the following 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, spraying cooling carried out in chilling tower,
(2) partial thermal decomposition gas carries out purified treatment into cleaning system, the wherein H of the pyrolysis after treatment2S and CO2Reach product
Product gas requirement, sour gas enters sulphur recovery unit, carries out sulphur recovery treatment；Partial thermal decomposition gas is removed by iron oxide process
Sour gas therein；
(3) coal tar that cooling is reclaimed carries out pre- hydrogenation lighting by entering suspended-bed reactor after dewater treatment
Treatment；
(4) oil product after processing fixed bed hydrogenation refining reaction and is hydrocracked anti-by entering after filtration treatment
Device is answered, the product oil of different fractions is produced；
(5) after the gas process after fixed bed hydrogenation treatment proposes hydrogen treatment, sour gas is directly entered sulphur recovery
Unit is processed；
(6) iron oxide process treatment contains H2As catalyst after iron sulfide is converted to after the sour gas of S by crushing
Participate in coal tar hydrogenating lighting reaction.
Such as Fig. 2, low-order coal described in the utility model includes following unit and process, unit bag using process
Include：Fast pyrogenation stove, separator, cooling tower, absorption tower, regenerator, sulphur recovery, adsorption tower, pulverizer, splitter box, suspension
Bed, filter, fixed bed, gas-liquid separator, carry hydrogen.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, is passed through
Low order fine coal is changed into and obtains through refining coal after pyrolysis, is discharged as product by fast pyrogenation stove bottom；
Pyrolysis oil gas from the discharge of fast pyrogenation furnace upper end is pyrolyzed oil gas by entering cooling tower after filtering in cooling tower
Enter in tower from cooling tower lower end, cooling water enters tower with the pyrolysis oil circulation of vital energy in the wrong direction to cooling is contacted from upper end, without the gas for cooling down
Cooling tower is discharged from tower top, the oil water mixture after cooling is flowed out by bottom of towe；
Pyrolysis gas and through carrying hydrogen treatment after partial hydrogenation reaction end gas mixing after by have absorption tower lower end enter,
Desulfurization solvent flows into absorption tower by tower top, and being contacted with back flow of gas carries out removing acidic components reaction, the product gas after reaction
Discharged by tower top, the desulfuration solution for absorbing sour gas enters regenerator；
The partial hydrogenation reaction end gas that pyrolysis gas and process are carried after hydrogen treatment are entered after mixing by adsorption tower upper end, only
Gas after change is discharged into product gas pipeline by tower bottom；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regeneration returns to 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 uses Complexing Iron sulphur recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Desulfuration adsorbent (iron oxide) in adsorption tower after adsorption saturation, powder is carried out after being discharged through bottom of towe into pulverizer
Enter suspension bed as catalyst after broken；
The mixture of coal tar and water after the cooling discharged by cooling tower bottom enters surge tank, carries out water-oil separating, point
Coal tar after enters floating bed hydrogenation unit；
Hydrogen, catalyst and coal tar carry out pre-hydrotreating into suspension bed together, and the gas after hydrogenation is from suspension
Bed tower top discharge, by the oil product after pre-hydrotreating by entering next unit after filtering；
The pre- oil product that is hydrogenated with passes through after filtering, and liquid-phase product enters fixed bed hydrogenation unit, while filtering consolidating for generation
Phase product is used as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering carries out hydrofinishing and hydrocracking reaction into fixed bed hydrogenation reactor,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase carries hydrogen production device, hydrogen as light-end products product, gas entrance
Can recycle, tail gas enters absorption tower.
The utility model utilizes tail gas produced during pyrolysis of coal process and coal tar hydrogenating in batches, in treatment acid
Property gas on the basis of again enable to treatment after adsorbent as the catalyst of coal tar suspension bed pre-hydrotreating, reach
The effect and purpose of comprehensive utilization are arrived.
Below with reference to specific embodiment, the utility model is described, it is necessary to explanation is, these embodiments are only
Descriptive, and the utility model is limited never in any form.
Embodiment 1
The present embodiment proposes a kind of system for processing coal tar, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery
Unit, catalyst preparation unit and pyrolysis oil vapor treatment unit：
Low order fine coal particle diameter (≤3mm), is pyrolyzed in down-flow fluidized bed using ECT, and lower formation temperature control is 700 DEG C, and pyrolysis oil gas is mixed
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, is changed into by low order fine coal after pyrolysis and is obtained through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Pyrolysis oil gas from the discharge of fast pyrogenation furnace upper end is pyrolyzed oil gas by entering cooling tower after filtering in cooling tower
Enter in 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, the tower after cooling treatment
At 80 DEG C, the gas without cooling discharges cooling tower to the temperature control at bottom from tower top, and the oil water mixture after cooling is by bottom of towe
Outflow；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by absorption tower lower end are carried after hydrogen treatment accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, and being contacted with back flow of gas carries out removing acidic components reaction, reacts it
Product gas afterwards are by the sulfur content≤20ppm, CO in tower top discharge product gas2≤ 2%, absorb the desulfuration solution of sour gas
Into regenerator；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by adsorption tower top are carried after hydrogen treatment accounts for total gas
The 0.5% of amount, is discharged, into product gas pipeline by the gas after purification by bottom of towe；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regeneration returns to 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 uses Complexing Iron sulphur recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, with hydrogen, coal tar after pulverizer is crushed
Enter floating bed hydrogenation reactor after oil mixing, the mass ratio of adsorbent and coal tar into the unit is 3:100；
The mixture of coal tar and water after the cooling discharged by cooling tower bottom enters surge tank, carries out water-oil separating, point
Coal tar after enters floating bed hydrogenation unit；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar carry out pre-hydrotreating into suspension bed together, urge
Agent accounts for the 2% of tar stock quality, and hydrogen is 1200 with the volume ratio of tar:1.Gas after hydrogenation is from suspension bed tower top
Discharge, by the oil product after pre-hydrotreating by entering next unit after filtering；
The pre- oil product that is hydrogenated with passes through after filtering, and liquid-phase product enters fixed bed hydrogenation unit, while filtering consolidating for generation
Phase product is used as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering carries out hydrofinishing and hydrocracking reaction into fixed bed hydrogenation reactor,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase carries hydrogen production device, hydrogen as light-end products product, gas entrance
Can recycle, sour gas enters absorption tower.
Embodiment 2
The present embodiment is as the system for use in carrying of above-described embodiment 1, 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 lower formation temperature control is 500 DEG C, and pyrolysis oil gas is mixed
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, is changed into by low order fine coal after pyrolysis and is obtained through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Pyrolysis oil gas from the discharge of fast pyrogenation furnace upper end is pyrolyzed oil gas by entering cooling tower after filtering in cooling tower
Enter in 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, the tower after cooling treatment
At 70 DEG C, the gas without cooling discharges cooling tower to the temperature control at bottom from tower top, and the oil water mixture after cooling is by bottom of towe
Outflow；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by absorption tower lower end are carried after hydrogen treatment accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, and being contacted with back flow of gas carries out removing acidic components reaction, reacts it
Product gas afterwards are by the sulfur content≤20ppm, CO in tower top discharge product gas2≤ 2%, absorb the desulfuration solution of sour gas
Into regenerator；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by adsorption tower top are carried after hydrogen treatment accounts for total gas
The 0.5% of amount, is discharged, into product gas pipeline by the gas after purification by bottom of towe；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regeneration returns to 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 uses Complexing Iron sulphur recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, with hydrogen, coal tar after pulverizer is crushed
Enter floating bed hydrogenation reactor after oil mixing, the mass ratio of adsorbent and coal tar into the unit is 3:100；
The mixture of coal tar and water after the cooling discharged by cooling tower bottom enters surge tank, carries out water-oil separating, point
Coal tar after enters floating bed hydrogenation unit；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar carry out pre-hydrotreating into suspension bed together, urge
Agent accounts for the 4% of tar stock quality, and hydrogen is 1500 with the volume ratio of tar:1.Gas after hydrogenation is from suspension bed tower top
Discharge, by the oil product after pre-hydrotreating by entering next unit after filtering；
The pre- oil product that is hydrogenated with passes through after filtering, and liquid-phase product enters fixed bed hydrogenation unit, while filtering consolidating for generation
Phase product is used as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering carries out hydrofinishing and hydrocracking reaction into fixed bed hydrogenation reactor,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase carries hydrogen production device, hydrogen as light-end products product, gas entrance
Can recycle, sour gas enters absorption tower.
Embodiment 3
The present embodiment is as the system for use in carrying of above-described embodiment 1, 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 lower formation temperature control is 900 DEG C, and pyrolysis oil gas is mixed
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, is changed into by low order fine coal after pyrolysis and is obtained through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Pyrolysis oil gas from the discharge of fast pyrogenation furnace upper end is pyrolyzed oil gas by entering cooling tower after filtering in cooling tower
Enter in 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, the tower after cooling treatment
At 90 DEG C, the gas without cooling discharges cooling tower to the temperature control at bottom from tower top, and the oil water mixture after cooling is by bottom of towe
Outflow；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by absorption tower lower end are carried after hydrogen treatment accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, and being contacted with back flow of gas carries out removing acidic components reaction, reacts it
Product gas afterwards are by the sulfur content≤20ppm, CO in tower top discharge product gas2≤ 2%, absorb the desulfuration solution of sour gas
Into regenerator；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by adsorption tower top are carried after hydrogen treatment accounts for total gas
The 0.4% of amount, is discharged, into product gas pipeline by the gas after purification by bottom of towe；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regeneration returns to 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 uses Complexing Iron sulphur recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, with hydrogen, coal tar after pulverizer is crushed
Enter floating bed hydrogenation reactor after oil mixing, the mass ratio of adsorbent and coal tar into the unit is 3:120；
The mixture of coal tar and water after the cooling discharged by cooling tower bottom enters surge tank, carries out water-oil separating, point
Coal tar after enters floating bed hydrogenation unit；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar carry out pre-hydrotreating into suspension bed together, urge
Agent accounts for the 1% of tar stock quality, and hydrogen is 2000 with the volume ratio of tar:1.Gas after hydrogenation is from suspension bed tower top
Discharge, by the oil product after pre-hydrotreating by entering next unit after filtering；
The pre- oil product that is hydrogenated with passes through after filtering, and liquid-phase product enters fixed bed hydrogenation unit, while filtering consolidating for generation
Phase product is used as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering carries out hydrofinishing and hydrocracking reaction into fixed bed hydrogenation reactor,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase carries hydrogen production device, hydrogen as light-end products product, gas entrance
Can recycle, sour gas enters absorption tower.
Embodiment 4
The present embodiment is as the system for use in carrying of above-described embodiment 1, 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 lower formation temperature control is 800 DEG C, and pyrolysis oil gas is mixed
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, is changed into by low order fine coal after pyrolysis and is obtained through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Pyrolysis oil gas from the discharge of fast pyrogenation furnace upper end is pyrolyzed oil gas by entering cooling tower after filtering in cooling tower
Enter in 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, the tower after cooling treatment
At 80 DEG C, the gas without cooling discharges cooling tower to the temperature control at bottom from tower top, and the oil water mixture after cooling is by bottom of towe
Outflow；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by absorption tower lower end are carried after hydrogen treatment accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, and being contacted with back flow of gas carries out removing acidic components reaction, reacts it
Product gas afterwards are by the sulfur content≤20ppm, CO in tower top discharge product gas2≤ 2%, absorb the desulfuration solution of sour gas
Into regenerator；
The hydrogenation reaction tail gas gaseous mixture that the pyrolysis gas and process entered by adsorption tower top are carried after hydrogen treatment accounts for total gas
The 0.6% of amount, is discharged, into product gas pipeline by the gas after purification by bottom of towe；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regeneration returns to 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 uses Complexing Iron sulphur recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, hydrogen sulfide is changed into elemental sulfur and is discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, with hydrogen, coal tar after pulverizer is crushed
Enter floating bed hydrogenation reactor after oil mixing, the mass ratio of adsorbent and coal tar into the unit is 3:90；
The mixture of coal tar and water after the cooling discharged by cooling tower bottom enters surge tank, carries out water-oil separating, point
Coal tar after enters floating bed hydrogenation unit；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar carry out pre-hydrotreating into suspension bed together, urge
Agent accounts for the 5% of tar stock quality, and hydrogen is 800 with the volume ratio of tar:1.Gas after hydrogenation is from suspension bed tower top
Discharge, by the oil product after pre-hydrotreating by entering next unit after filtering；
The pre- oil product that is hydrogenated with passes through after filtering, and liquid-phase product enters fixed bed hydrogenation unit, while filtering consolidating for generation
Phase product is used as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering carries out hydrofinishing and hydrocracking reaction into fixed bed hydrogenation reactor,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase carries hydrogen production device, hydrogen as light-end products product, gas entrance
Can recycle, sour gas enters absorption tower.
Although embodiment of the present utility model has been shown and described above, it is to be understood that above-described embodiment is
Exemplary, it is impossible to it is interpreted as to limitation of the present utility model, one of ordinary skill in the art is in scope of the present utility model
It is interior above-described embodiment to be changed, changed, replaced and modification.
What the utility model disclosure was touched upon is exemplary embodiment, is not departing from the protection that claims are defined
In the case of scope, each embodiment of the application can be made various changes and modifications.Therefore, described embodiment purport
Covering to fall all such changes, modifications and deformation in the protection domain of appended claims.Additionally, except context is another
Outside alluding to, the word for occurring in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then Ren Heshi
Apply example all or part of can combine any other embodiment all or part of use.
Claims (6)
1. a kind of system of utilization low-order coal, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery unit, catalyst preparation
Unit and pyrolysis oil vapor treatment unit；Wherein,
The pyrolysis unit includes low order coal powder entrance, obtains through refining coal export, the outlet of the first pyrolysis gas, the outlet of the second pyrolysis gas
With coal tar oil export after water-oil separating, the pyrolysis unit be used for low order coal dust pyrolysis, pyrolysis hydrocarbon filter and cooling and
The separation of oil water mixture；
The desulfurization and decarburization unit include the first pyrolysis gas entrance, oil vapor treatment after gas inlet, desulfurization and decarburization solution inlet,
Sour gas outlet after first product gas outlet and desulfurization and decarburization, the desulfurization and decarburization unit is used to for gas to carry out desulfurization and decarburization
Treatment obtains product gas；
The sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet, the sulphur recovery after desulfurization and decarburization
Unit is used for after desulfurization and decarburization the recovery of hydrogen sulfide in sour gas, and hydrogen sulfide is further transformed to elemental sulfur；
The catalyst preparation unit includes the second pyrolysis gas entrance, the second product gas outlet and catalyst outlet, described
Catalyst preparation unit is adsorbed with desulfuration adsorbent to sour gas, and the adsorbent after adsorption saturation is used as the pyrolysis oil
The catalyst of gas disposal unit；
The pyrolysis oil vapor treatment unit includes coal tar oil-in, hydrogen inlet, catalyst inlet, light-end products after water-oil separating
Offgas outlet after product exit and oil vapor treatment, the pyrolysis oil vapor treatment unit is used for the anti-of hydrogen, catalyst and coal tar
Should, tail gas after light-end products product and oil vapor treatment is obtained, tail gas enters at the desulfurization and decarburization unit continuation after oil vapor treatment
Reason；
The first pyrolysis gas outlet is connected with the first pyrolysis gas entrance, and second pyrolysis gas are exported and described
Second pyrolysis gas entrance is connected, and coal tar oil export is connected with coal tar oil-in after the water-oil separating after the water-oil separating,
Gas inlet is connected with offgas outlet after the oil vapor treatment after the oil vapor treatment, sour gas outlet after the desulfurization and decarburization
It is connected with sour gas entrance after the desulfurization and decarburization, catalyst outlet described in the catalyst inlet is connected.
2. system according to claim 1, it is characterised in that
The pyrolysis unit is connected by fast pyrogenation stove, separator, cooling tower with splitter box order：
The fast pyrogenation stove is used for the pyrolysis of low order coal dust；
The separator is used to be pyrolyzed the separation of gas phase liquid phase and solid phase in oil gas；
The pyrolysis oil gas after by filtering used for cooling tower is cooled down, and obtains pyrolysis gas into the desulfurization and decarburization list
Unit, the oil water mixture for obtaining enters the splitter box；
The splitter box is used to be separated the oil water mixture after cooling, obtains the coal tar after water-oil separating and enters described
Pyrolysis oil vapor treatment unit.
3. system according to claim 1, it is characterised in that
The desulfurization and decarburization unit includes absorption tower and regenerator：
The absorption tower is used to for the gas from the pyrolysis unit and the pyrolysis oil vapor treatment unit to carry out desulfurization and decarburization
Reaction, the desulfurization and decarburization solution for absorbing sour gas enters the regenerator；
The regenerator carries out regeneration treatment to the desulfurization and decarburization solution for absorbing sour gas, and the solvent after regeneration is returned
Go back to absorption tower to recycle, regenerator tower overhead gas enters the sulphur recovery unit.
4. system according to claim 1, it is characterised in that
The sulphur recovery unit includes sulfur recovery facility and baker：
The sulfur recovery facility uses Complexing Iron sulphur recovery solution, reclaims the hydrogen sulfide in sour gas, hydrogen sulfide transformation
For elemental sulfur is discharged by bottom of towe；
The baker is used to be dried the elemental sulfur that bottom of towe is discharged.
5. system according to claim 1, it is characterised in that
The catalyst preparation unit includes adsorption tower and pulverizer：
The adsorption tower with iron oxide as adsorbent, for being adsorbed to the sour gas for coming from the pyrolysis unit；
The pulverizer is used to crush the adsorbent after adsorption saturation, and the pyrolysis is entered as catalyst after crushing
Oil vapor treatment unit.
6. system according to claim 1, it is characterised in that
The pyrolysis oil vapor treatment unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries hydrogen production device：
The suspension bed be used for hydrogen, catalyst and coal tar are carried out into pre-hydrotreating, the gas for obtaining from tower top discharge into
Hydrogen production device is carried described in entering, the oil product for obtaining enters the filter；
The filter is used to be filtered the oil product obtained after pre-hydrotreating, while filtering the solids product conduct for producing
Outer whipping slag discharge filter；
The fixed bed is used to for the oil product from the filter to carry out hydrofinishing and hydrocracking reaction, after reaction
Liquid phase product enters the gas-liquid separator；
The gas-liquid separator is used to be separated reacted liquid phase product, and the liquid phase for obtaining is produced as light-end products
Thing, the gas for obtaining carries hydrogen production device described in；
The hydrogen obtained after hydrogen production device processing gas that carries is recycled into the suspension bed, and the sour gas for obtaining enters
The desulfurization and decarburization unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621126092.9U CN206279155U (en) | 2016-10-14 | 2016-10-14 | A kind of system of utilization low-order coal |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621126092.9U CN206279155U (en) | 2016-10-14 | 2016-10-14 | A kind of system of utilization low-order coal |
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| CN206279155U true CN206279155U (en) | 2017-06-27 |
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| CN201621126092.9U Withdrawn - After Issue CN206279155U (en) | 2016-10-14 | 2016-10-14 | A kind of system of utilization low-order coal |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318430B (en) * | 2016-10-14 | 2018-03-23 | 神雾科技集团股份有限公司 | A kind of system and method using low-order coal |
| CN113122345A (en) * | 2019-12-30 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for treating high-sulfur natural gas |
-
2016
- 2016-10-14 CN CN201621126092.9U patent/CN206279155U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318430B (en) * | 2016-10-14 | 2018-03-23 | 神雾科技集团股份有限公司 | A kind of system and method using low-order coal |
| CN113122345A (en) * | 2019-12-30 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for treating high-sulfur natural gas |
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Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee 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 Patentee before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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