CN106318430B - A kind of system and method using low-order coal - Google Patents
A kind of system and method using low-order coal Download PDFInfo
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- CN106318430B CN106318430B CN201610899948.4A CN201610899948A CN106318430B CN 106318430 B CN106318430 B CN 106318430B CN 201610899948 A CN201610899948 A CN 201610899948A CN 106318430 B CN106318430 B CN 106318430B
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- 239000003245 coal Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 191
- 238000000197 pyrolysis Methods 0.000 claims abstract description 141
- 235000019198 oils Nutrition 0.000 claims abstract description 126
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 103
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 80
- 230000023556 desulfurization Effects 0.000 claims abstract description 69
- 239000001257 hydrogen Substances 0.000 claims abstract description 68
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 68
- 238000001816 cooling Methods 0.000 claims abstract description 67
- 238000011084 recovery Methods 0.000 claims abstract description 66
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 65
- 238000005261 decarburization Methods 0.000 claims abstract description 63
- 239000011280 coal tar Substances 0.000 claims abstract description 60
- 238000011282 treatment Methods 0.000 claims abstract description 56
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 239000003463 adsorbent Substances 0.000 claims abstract description 36
- 239000005864 Sulphur Substances 0.000 claims abstract description 35
- 238000001179 sorption measurement Methods 0.000 claims abstract description 33
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 239000000725 suspension Substances 0.000 claims abstract description 26
- 235000019476 oil-water mixture Nutrition 0.000 claims abstract description 21
- 238000002360 preparation method Methods 0.000 claims abstract description 18
- 239000002817 coal dust Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 4
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 4
- 239000000047 product Substances 0.000 claims description 107
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 50
- 238000001914 filtration Methods 0.000 claims description 36
- 238000010521 absorption reaction Methods 0.000 claims description 33
- 239000007791 liquid phase Substances 0.000 claims description 28
- 238000004519 manufacturing process Methods 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 20
- 150000002431 hydrogen Chemical class 0.000 claims description 17
- 230000032258 transport Effects 0.000 claims description 15
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 14
- 238000007670 refining Methods 0.000 claims description 13
- 239000002904 solvent Substances 0.000 claims description 13
- 239000007795 chemical reaction product Substances 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 12
- 229910052717 sulfur Inorganic materials 0.000 claims description 12
- 230000008929 regeneration Effects 0.000 claims description 11
- 238000011069 regeneration method Methods 0.000 claims description 11
- 239000011593 sulfur Substances 0.000 claims description 11
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 claims description 10
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 9
- 230000000536 complexating effect Effects 0.000 claims description 9
- 239000012071 phase Substances 0.000 claims description 9
- 239000002893 slag Substances 0.000 claims description 9
- 230000001172 regenerating effect Effects 0.000 claims description 7
- 239000000843 powder Substances 0.000 claims description 4
- 241000748712 Colias canadensis Species 0.000 claims description 2
- 239000007790 solid phase Substances 0.000 claims description 2
- 238000004073 vulcanization Methods 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 230000009466 transformation Effects 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 47
- 239000011269 tar Substances 0.000 abstract description 28
- 230000008569 process Effects 0.000 abstract description 26
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 99
- 238000007667 floating Methods 0.000 description 10
- 239000008246 gaseous mixture Substances 0.000 description 8
- 238000002156 mixing Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 5
- 239000000428 dust Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 208000006558 Dental Calculus Diseases 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000011287 low-temperature tar Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- -1 semicoke Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
- B01D2253/1124—Metal oxides
Abstract
The present invention discloses a kind of system and method using 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 pyrolysis, pyrolysis hydrocarbon filter and cooling and the separation of oil water mixture of low order coal dust；Desulfurization and decarburization unit is used to handle to obtain product gas by gas progress desulfurization and decarburization；Recovery of the sulphur recovery unit for hydrogen sulfide in sour gas after desulfurization and decarburization, hydrogen sulfide are 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；It is pyrolyzed the reaction that oil vapor treatment unit is used for hydrogen, catalyst and coal tar.The present invention can make full use of sour gas caused by pyrolysis of coal process and hydrogenation of tar process, and complete the preparation of coal tar suspension bed hydrogenation pretreatment catalyst while sour gas is handled by adsorbent.
Description
Technical field
The invention belongs to coal processing technology field, more particularly to a kind of system and method using low-order coal.
Background technology
Coal sub-prime is using being considered as effective way that Coal Clean efficiently utilizes, and 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, which utilizes, 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 instead of dissipating and reduce pollution to air.
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 utilizes
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 utilizes, soon
Speed heat solution typically handles fine coal raw material, and fine coal temperature rise in pyrolysis oven is fast, 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 and cold tar in tar
Receive in tower and carry out contact heat-exchanging, reclaim the tar condensing in pyrolysis gas, 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 is recycled back to tar recovery tower bottom, improves tar and returned in tar
The flow velocity of tower bottom is received, prevents dust deposit from blocking recovery tower.The invention is used as cooling medium, part heavy by the use of heavy tar
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.In addition, tar recovery tower upper end is equipped with filler in this 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 this method is by coalite tar
Or its bottoms adds in feed coal and carries out copyrolysis, obtains the preparation method of tar and gaseous hydrocarbon product.Specific method is
Coalite tar or its bottoms are uniformly mixed with feed coal, enter copyrolysis in pyrolysis oven jointly, obtains liquid
Product, pyrolysis gas, semicoke, product liquid are oil water mixture, and coalite tar is obtained after water-oil separating.Low temperature in the 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 into block or mud
Shape, difficulty is brought to the processing such as material screening, broken.In addition, pyrolysis oil gas uses water cooling, large amount of sewage, while heat can be produced
Solution oil gas heat does not also utilize effectively.
The content of the invention
The present invention has coupled the fast pyrogenation, pyrolysis oil vapor treatment and caused acid tail gas processing work during this of coal
Skill.Aim to provide it is a kind of using low order fine coal fast pyrogenation as source, pyrolysis oil gas efficiently utilize and sour gas rationally return
Receive the coal high-efficiency classified utilization technique of processing.The technique can be produced high-quality using low-order coal as raw material and obtain through refining coal, cleaning
Liquid fuel, and pyrolytic process can be recycled and petroleum resources cleans the miscellaneous elements such as S, N in processing procedure, accomplish
It is environment-friendly, output resource rational utilization.
To achieve the above object, the present invention proposes a kind of system using 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 second pyrolysis gas
Coal tar oil export behind outlet and water-oil separating, the pyrolysis unit are used for pyrolysis, pyrolysis hydrocarbon filter and the cooling of low order coal dust
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
Sour gas exports after entrance, the first product gas outlet and desulfurization and decarburization, and the desulfurization and decarburization unit is used to enter sour gas
Row desulfurization and decarburization handles to obtain product gas；
The sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet after desulfurization and decarburization, the sulphur
Recovery of the recovery unit for hydrogen sulfide in sour gas after desulfurization and decarburization, hydrogen sulfide are 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 after water-oil separating, catalyst inlet, lightweight
Offgas outlet after oil product product exit and oil vapor treatment, the pyrolysis oil vapor treatment unit are 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 processing；
First pyrolysis gas outlet is connected with the first pyrolysis gas entrance, the second pyrolysis gas outlet 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 for the separation for being pyrolyzed gas phase liquid phase and solid phase in oil gas；
The pyrolysis oil gas used for cooling tower after by filtering is cooled down, and is obtained pyrolysis gas and is entered the desulfurization and decarburization
Unit, obtained oil water mixture enter 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 the gas from the pyrolysis unit and the pyrolysis oil vapor treatment unit carrying out desulfurization
Decarburizing reaction, the desulfurization and decarburization solution for absorbing sour gas enter the regenerator；
The regenerator carries out regeneration treatment to the desulfurization and decarburization solution for absorbing sour gas, molten after regenerating
Agent returns to absorption tower and recycled, 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 the elemental sulfur of bottom of towe discharge being dried.
Specifically, the catalyst preparation unit includes adsorption tower and pulverizer：
The adsorption tower is using 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, as described in catalyst entrance after crushing
It is pyrolyzed oil vapor treatment unit.
Further, the pyrolysis oil vapor treatment unit includes suspension bed, filter, fixed bed, gas-liquid separator and carried
Hydrogen production device：
The suspension bed is used to hydrogen, catalyst and coal tar carrying out pre-hydrotreating, and obtained gas is arranged from tower top
Go out and carry hydrogen production device described in entering, obtained oil product enters the filter；
The filter is used to be filtered the oil product obtained after pre-hydrotreating, while solids product caused by filtering
As outer whipping slag discharge filter；
The fixed bed is used to the oil product from the filter carrying 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 obtained liquid phase is as light-end products
Product, obtained gas enter described in carry hydrogen production device；
The hydrogen obtained after hydrogen production device processing gas that carries recycles into the suspension bed, obtained sour gas
Into the desulfurization and decarburization unit.
The present invention also provides a kind of method using low-order coal, comprises the following steps：
A. it is pyrolyzed：First low order coal dust is pyrolyzed in the pyrolysis unit, then carried out obtained pyrolysis oil gas
Filter and cooling, obtain pyrolysis gas and oil water mixture, are finally separated the oil water mixture；
B. desulfurization and decarburization：Sour gas progress desulfurization and decarburization is handled to obtain product gas and taken off in the desulfurization and decarburization unit
Sour gas after sulphur decarburization；
C. sulphur recovery：Sour gas carries out vulcanization hydrogen retrieval after the sulphur recovery unit is to the desulfurization and decarburization,
The hydrogen sulfide is changed into elemental sulfur；
D. catalyst preparation：Sour gas is adsorbed with desulfuration adsorbent in the catalyst preparation unit, will be inhaled
Adsorbent after attached saturation is used as the catalyst of the pyrolysis oil vapor treatment unit；
E. it is pyrolyzed oil vapor treatment：The reaction of hydrogen, catalyst and coal tar is carried out in the pyrolysis oil vapor treatment unit, is obtained
Tail gas after to light-end products product and oil vapor treatment, tail gas after the oil vapor treatment is transported into the desulfurization and decarburization unit and continues to locate
Reason.
Further, in the step A, low order coal dust is first placed in the fast pyrogenation stove and is pyrolyzed, is pyrolyzed it
The coal of obtaining through refining obtained afterwards is discharged by furnace bottom, and the pyrolysis oil gas is obtained after pyrolysis and transports to the separator gas-liquid-solid is divided
From；
Then the pyrolysis oil gas after filtering is cooled down in the cooling tower, obtains the pyrolysis gas and transport to described take off
Sulphur decarburization unit, the obtained oil water mixture transport to the splitter box；
Finally the oil water mixture after cooling is separated in the splitter box, obtains the coal tar after water-oil separating
Oil transports to the pyrolysis oil vapor treatment unit.
Preferably, the size controlling of the low order fine coal is existed less than or equal to 3mm, the fast pyrogenation stove control
500~900 DEG C, the temperature control at the cooling tower bottom is at 70~90 DEG C.
Specifically, in the step B, will first be come from the absorption tower at the pyrolysis unit and the pyrolysis oil gas
The gas for managing unit carries out desulfurization and decarburization reaction, and the product gas after reacting is discharged by tower top, absorbs the desulfurization of sour gas
Decarbonizing solution transports to the regenerator, then regeneration treatment is carried out to desulfurization and decarburization solution in the regenerator, after regeneration
Solvent transport to absorption tower recycling, regenerator tower overhead gas transports to the sulphur recovery unit.
Further, in the step C, first in the sulfur recovery facility using Complexing Iron sulphur as recovery solution,
The hydrogen sulfide in sour gas is reclaimed using self-loopa recovery process, the hydrogen sulfide is changed into elemental sulfur and discharged by bottom of towe, so
Afterwards the elemental sulfur that bottom of towe is discharged is dried to obtain elemental sulfur in the baker.
Specifically, in the step D, first using iron oxide as adsorbent in the adsorption tower, to coming from the heat
The gas of solution unit is adsorbed, and obtains product gas；Then the adsorbent after adsorption saturation is subjected to powder in the pulverizer
It is broken, transport to the pyrolysis oil vapor treatment unit using the adsorbent after crushing as catalyst.
Further, in the step E, first hydrogen, catalyst and coal tar are hydrogenated with advance in the suspension bed
Processing, by obtained gas from tower top discharge transport to it is described carry hydrogen production device, obtained oil product is transported to the filter and filtered,
Filtering is with caused solids product as outer whipping slag discharge filter；
Then hydrofinishing and hydrocracking reaction are carried out to the oil product after filtering in the fixed bed, after reaction
Liquid phase product transports to the gas-liquid separator；
Subsequently reacted liquid phase product is separated in the gas-liquid separator, obtained liquid phase is lightweight
Oil product product, obtained gas, which is transported to, described carries hydrogen production device；
Finally after hydrogen production device is carried to gas treatment, obtained hydrogen is transported into the suspension bed and recycled, is obtained
Sour gas is transported to the desulfurization and decarburization unit and further handled.
Preferably, the catalyst accounts for the 1~5% of the coal tar oil quality, the volume of the hydrogen and the coal tar
Than for 800~2000:1.
The present invention can make full use of sour gas caused by pyrolysis of coal process and hydrogenation of tar process, and pass through adsorbent
The preparation of coal tar suspension bed hydrogenation pretreatment catalyst is completed while sour gas is handled.In addition, the present invention can
Acid tail gas caused by pyrolysis of coal, floating bed hydrogenation, oil refinery is uniformly processed, recycled.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Brief description of the drawings
The low-order coal that Fig. 1 is the present invention utilizes system structure diagram.
The low-order coal that Fig. 2 is the present invention utilizes process chart.
Embodiment
Below in conjunction with drawings and examples, the embodiment of the present invention is described in more details, so as to energy
The advantages of enough more fully understanding the solution of the present invention and its various aspects.However, specific embodiments described below and implementation
Example is for illustrative purposes only, rather than limitation of the present invention.
The present invention is that fine coal carries out obtaining through refining processing 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 after being handled through electrically trapped tar oil device, produce pure pyrolysis gas and enter downstream
Handling process.Pyrolytic tar carries out just hydrotreating by suspension bed, and it is different that light components enter fixed bed deep processing production
The various distillate fuel oils of cut.
Low-order coal handling process of the present invention, is mainly included the following steps that：
(1) fine coal enters down-flow fluidized bed using ECT pyrolysis oven, and it is laggard that caused pyrolysis oil gas removing dust device removes bulky grain mechanical admixture
Enter chilling tower, spraying cooling carried out in chilling tower,
(2) partial thermal decomposition gas enters cleaning system progress purified treatment, the pyrolysis wherein H after handling2S and CO2Reach production
The requirement of product gas, sour gas enter sulphur recovery unit, carry out sulphur recovery processing；Partial thermal decomposition gas is removed by iron oxide process
Sour gas therein；
(3) coal tar of cooling recovery carries out pre- hydrogenation lighting by entering suspended-bed reactor after dewater treatment
Processing；
(4) oil product after handling fixed bed hydrogenation refining reaction and is hydrocracked anti-by entering after filtration treatment
Device is answered, produces the product oil of different fractions；
(5) for the gas after fixed bed hydrogenation processing after proposing hydrogen processing, sour gas is directly entered sulphur recovery
Unit is handled；
(6) iron oxide process processing contains H2Iron sulfide is converted to after S sour gas and is used as catalyst after crushing
Participate in coal tar hydrogenating lighting reaction.
Such as Fig. 2, low-order coal of the present invention includes following unit and process using process, and unit includes：It hurry up
Fast pyrolysis oven, separator, cooling tower, absorption tower, regenerator, sulphur recovery, adsorption tower, pulverizer, splitter box, suspension bed, mistake
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, which is changed into, after pyrolysis obtains through refining coal, is discharged by fast pyrogenation stove bottom as product；
Enter cooling tower after filtering from the pyrolysis oil gas of fast pyrogenation furnace upper end discharge, oil gas is pyrolyzed in cooling tower
Enter from cooling tower lower end in tower, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction from upper end and cooled to contacting, the gas without cooling
Cooling tower is discharged from tower top, the oil water mixture after cooling down is flowed out by bottom of towe；
Pyrolysis gas and through carrying hydrogen processing after partial hydrogenation reaction end gas mixing after by have absorption tower lower end entrance,
Desulfurization solvent flows into absorption tower by tower top, is contacted with back flow of gas and carries out removing acidic components reaction, the product gas after reacting
Discharged by tower top, the desulfuration solution for absorbing sour gas enters regenerator；
Pyrolysis gas and process are entered after proposing the partial hydrogenation reaction end gas mixing after hydrogen processing 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 regenerating 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 discharged by bottom of towe；
Desulfuration adsorbent (iron oxide) in adsorption tower after adsorption saturation, pulverizer progress powder is entered after bottom of towe is discharged
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
Enter floating bed hydrogenation unit from coal tar afterwards；
Hydrogen, catalyst and coal tar enter suspension bed and carry out pre-hydrotreating together, and gas after being hydrogenated with is from suspension
Bed tower top discharge, the oil product after pre-hydrotreating enter next unit after filtering；
For pre- hydrogenation oil product after filtering, liquid-phase product enters fixed bed hydrogenation unit, while solid caused by filtering
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and for liquid phase as light-end products product, gas, which enters, carries hydrogen production device, hydrogen
It can recycle, tail gas enters absorption tower.
The present invention utilizes caused tail gas during pyrolysis of coal process and coal tar hydrogenating in batches, in processing sour gas
Catalyst of the adsorbent after handling as coal tar suspension bed pre-hydrotreating is enabled on the basis of body again, is reached
The effect and purpose of comprehensive utilization.
Below with reference to specific embodiment, present invention is described, it is necessary to which explanation, these embodiments are only to describe
Property, without limiting the invention in any way.
Embodiment 1
The present embodiment proposes a kind of system for handling 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 mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and low order fine coal, which is changed into, after pyrolysis obtains through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Enter cooling tower after filtering from the pyrolysis oil gas of fast pyrogenation furnace upper end discharge, oil gas is pyrolyzed in cooling tower
Enter from cooling tower lower end in tower, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction from upper end and cooled to contacting, the tower after cooling is handled
The temperature control at bottom is at 80 DEG C, and the gas without cooling discharges cooling tower from tower top, and the oil water mixture after cooling down 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 is carried after hydrogen processing accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, is contacted with back flow of gas and carries out removing acidic components reaction, reacts it
Product gas afterwards is discharged sulfur content≤20ppm, CO in product gas by tower top2≤ 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 is carried after hydrogen processing accounts for total gas
The 0.5% of amount, the gas after purification is discharged by bottom of towe, into product gas pipeline；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regenerating 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 discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, after pulverizer crushes with hydrogen, coal tar
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
Enter floating bed hydrogenation unit from coal tar afterwards；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar enter suspension bed and carry out pre-hydrotreating together, urge
Agent accounts for the 2% of tar stock quality, and the volume ratio of hydrogen and tar is 1200:1.Gas after hydrogenation is from suspension bed tower top
Discharge, the oil product after pre-hydrotreating enter next unit after filtering；
For pre- hydrogenation oil product after filtering, liquid-phase product enters fixed bed hydrogenation unit, while solid caused by filtering
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and for liquid phase as light-end products product, gas, which enters, carries hydrogen production device, hydrogen
It 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 mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and low order fine coal, which is changed into, after pyrolysis obtains through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Enter cooling tower after filtering from the pyrolysis oil gas of fast pyrogenation furnace upper end discharge, oil gas is pyrolyzed in cooling tower
Enter from cooling tower lower end in tower, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction from upper end and cooled to contacting, the tower after cooling is handled
The temperature control at bottom is at 70 DEG C, and the gas without cooling discharges cooling tower from tower top, and the oil water mixture after cooling down 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 is carried after hydrogen processing accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, is contacted with back flow of gas and carries out removing acidic components reaction, reacts it
Product gas afterwards is discharged sulfur content≤20ppm, CO in product gas by tower top2≤ 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 is carried after hydrogen processing accounts for total gas
The 0.5% of amount, the gas after purification is discharged by bottom of towe, into product gas pipeline；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regenerating 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 discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, after pulverizer crushes with hydrogen, coal tar
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
Enter floating bed hydrogenation unit from coal tar afterwards；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar enter suspension bed and carry out pre-hydrotreating together, urge
Agent accounts for the 4% of tar stock quality, and the volume ratio of hydrogen and tar is 1500:1.Gas after hydrogenation is from suspension bed tower top
Discharge, the oil product after pre-hydrotreating enter next unit after filtering；
For pre- hydrogenation oil product after filtering, liquid-phase product enters fixed bed hydrogenation unit, while solid caused by filtering
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and for liquid phase as light-end products product, gas, which enters, carries hydrogen production device, hydrogen
It 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 mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and low order fine coal, which is changed into, after pyrolysis obtains through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Enter cooling tower after filtering from the pyrolysis oil gas of fast pyrogenation furnace upper end discharge, oil gas is pyrolyzed in cooling tower
Enter from cooling tower lower end in tower, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction from upper end and cooled to contacting, the tower after cooling is handled
The temperature control at bottom is at 90 DEG C, and the gas without cooling discharges cooling tower from tower top, and the oil water mixture after cooling down 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 is carried after hydrogen processing accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, is contacted with back flow of gas and carries out removing acidic components reaction, reacts it
Product gas afterwards is discharged sulfur content≤20ppm, CO in product gas by tower top2≤ 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 is carried after hydrogen processing accounts for total gas
The 0.4% of amount, the gas after purification is discharged by bottom of towe, into product gas pipeline；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regenerating 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 discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, after pulverizer crushes with hydrogen, coal tar
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
Enter floating bed hydrogenation unit from coal tar afterwards；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar enter suspension bed and carry out pre-hydrotreating together, urge
Agent accounts for the 1% of tar stock quality, and the volume ratio of hydrogen and tar is 2000:1.Gas after hydrogenation is from suspension bed tower top
Discharge, the oil product after pre-hydrotreating enter next unit after filtering；
For pre- hydrogenation oil product after filtering, liquid-phase product enters fixed bed hydrogenation unit, while solid caused by filtering
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and for liquid phase as light-end products product, gas, which enters, carries hydrogen production device, hydrogen
It 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 mixes
Compound is discharged by the exhaust outlet of down-flow fluidized bed using ECT upper end, and low order fine coal, which is changed into, after pyrolysis obtains through refining coal, by under fast pyrogenation stove
Discharged as product in portion；
Enter cooling tower after filtering from the pyrolysis oil gas of fast pyrogenation furnace upper end discharge, oil gas is pyrolyzed in cooling tower
Enter from cooling tower lower end in tower, cooling water enters tower and the pyrolysis oil circulation of vital energy in the wrong direction from upper end and cooled to contacting, the tower after cooling is handled
The temperature control at bottom is at 80 DEG C, and the gas without cooling discharges cooling tower from tower top, and the oil water mixture after cooling down 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 is carried after hydrogen processing accounts for total gas
The 99.5% of amount, desulfurization solvent flows into absorption tower by tower top, is contacted with back flow of gas and carries out removing acidic components reaction, reacts it
Product gas afterwards is discharged sulfur content≤20ppm, CO in product gas by tower top2≤ 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 is carried after hydrogen processing accounts for total gas
The 0.6% of amount, the gas after purification is discharged by bottom of towe, into product gas pipeline；
The desulfurization and decarburization solution of sour gas is absorbed, into regenerator, the solvent after regenerating 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 discharged by bottom of towe；
Adsorbent in adsorption tower after the adsorption of hydrogen sulfide saturation of discharge, after pulverizer crushes with hydrogen, coal tar
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
Enter floating bed hydrogenation unit from coal tar afterwards；
Hydrogen, catalyst (adsorbent of adsorption saturation) and coal tar enter suspension bed and carry out pre-hydrotreating together, urge
Agent accounts for the 5% of tar stock quality, and the volume ratio of hydrogen and tar is 800:1.Gas after hydrogenation is from suspension bed tower top
Discharge, the oil product after pre-hydrotreating enter next unit after filtering；
For pre- hydrogenation oil product after filtering, liquid-phase product enters fixed bed hydrogenation unit, while solid caused by filtering
Phase product is as outer whipping slag discharge filter；
Pre- hydrogenated products oil after filtering enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and for liquid phase as light-end products product, gas, which enters, carries hydrogen production device, hydrogen
It can recycle, sour gas enters absorption tower.
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 limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changed, replacing and modification.
What present disclosure referred to is exemplary embodiment, in the protection domain for not departing from claims and defining
In the case of, each embodiment of the application can be made various changes and modifications.Therefore, described embodiment is intended to contain
Lid falls all such changes, modifications and deformation in the protection domain of appended claims.In addition, institute unless the context
Outside referring to, the word occurred in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then any embodiment
All or part of can combine any other embodiment all or part of use.
Claims (10)
1. a kind of system using 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, gas inlet after oil vapor treatment, desulfurization and decarburization solution inlet,
Sour gas exports after first product gas outlet and desulfurization and decarburization, and the desulfurization and decarburization unit is used to gas carrying out desulfurization and decarburization
Processing obtains product gas；
The sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet after desulfurization and decarburization, the sulphur recovery
Recovery of the unit for hydrogen sulfide in sour gas after desulfurization and decarburization, hydrogen sulfide are 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 after water-oil separating, catalyst inlet, light-end products
Offgas outlet after product exit and oil vapor treatment, the pyrolysis oil vapor treatment unit are 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 continues to locate into the desulfurization and decarburization unit after oil vapor treatment
Reason；
First pyrolysis gas outlet is connected with the first pyrolysis gas entrance, the second pyrolysis gas outlet with it is 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, and sour gas exports 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 for the separation for being pyrolyzed gas phase liquid phase and solid phase in oil gas；
The pyrolysis oil gas used for cooling tower after by filtering is cooled down, and is obtained pyrolysis gas and is entered the desulfurization and decarburization list
Member, obtained oil water mixture enter the splitter box；
The splitter box is used to be separated the oil water mixture after cooling, obtains described in the entrance of the coal tar after water-oil separating
It is pyrolyzed 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 the gas from the pyrolysis unit and the pyrolysis oil vapor treatment unit carrying out desulfurization and decarburization
Reaction, the desulfurization and decarburization solution for absorbing sour gas enter the regenerator；
The regenerator carries out regeneration treatment to the desulfurization and decarburization solution for absorbing sour gas, and the solvent after regenerating returns
Go back to absorption tower to recycle, regenerator tower overhead gas enters the sulphur recovery unit；
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
Discharged for elemental sulfur by bottom of towe；
The baker is used to the elemental sulfur of bottom of towe discharge being dried.
4. system according to claim 1, it is characterised in that
The catalyst preparation unit includes adsorption tower and pulverizer：
The adsorption tower is using 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, enters the pyrolysis as catalyst after crushing
Oil vapor treatment unit.
5. 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 by hydrogen, catalyst and coal tar carry out pre-hydrotreating, obtained gas from tower top discharge into
Hydrogen production device is carried described in entering, obtained oil product enters the filter；
The filter is used to be filtered the oil product obtained after pre-hydrotreating, while solids product conduct caused by filtering
Outer whipping slag discharge filter；
The fixed bed is used to the oil product from the filter carrying out hydrofinishing and hydrocracking reaction, after reacting
Liquid phase product enters the gas-liquid separator；
The gas-liquid separator is used to be separated reacted liquid phase product, and obtained liquid phase is produced as light-end products
Thing, obtained gas enter described in carry hydrogen production device；
The hydrogen obtained after hydrogen production device processing gas that carries recycles into the suspension bed, and obtained sour gas enters
The desulfurization and decarburization unit.
6. a kind of method that system described in claim 1 utilizes low-order coal, it is characterised in that including step：
A. it is pyrolyzed：First low order coal dust is pyrolyzed in the pyrolysis unit, then by obtained pyrolysis oil gas carry out filtering and
Cooling, obtains pyrolysis gas and oil water mixture, is finally separated the oil water mixture；
B. desulfurization and decarburization：Sour gas progress desulfurization and decarburization is handled to obtain product gas in the desulfurization and decarburization unit and desulfurization takes off
Sour gas after carbon；
C. sulphur recovery：Sour gas carries out vulcanization hydrogen retrieval after the sulphur recovery unit is to the desulfurization and decarburization, described
Hydrogen sulfide is changed into elemental sulfur；
D. catalyst preparation：Sour gas is adsorbed with desulfuration adsorbent in the catalyst preparation unit, absorption is full
Adsorbent with after is used as the catalyst of the pyrolysis oil vapor treatment unit；
E. it is pyrolyzed oil vapor treatment：The reaction of hydrogen, catalyst and coal tar is carried out in the pyrolysis oil vapor treatment unit, is obtained light
Tail gas after matter oil product product and oil vapor treatment, tail gas after the oil vapor treatment is transported into the desulfurization and decarburization unit and continued with.
7. according to the method for claim 6, it is characterised in that
In the step A, low order coal dust is first placed in fast pyrogenation stove and is pyrolyzed, what pyrolysis obtained afterwards obtains through refining coal by stove
Bottom is discharged, and the pyrolysis oil gas is obtained after pyrolysis and transports to separator gas-liquid-solid is separated；
Then the pyrolysis oil gas after filtering is cooled down in cooling tower, obtains the pyrolysis gas and transport to the desulfurization and decarburization list
Member, the obtained oil water mixture transport to splitter box；
Finally the oil water mixture after cooling is separated in the splitter box, it is defeated to obtain the coal tar after water-oil separating
To the pyrolysis oil vapor treatment unit；
By the size controlling of the low order fine coal less than or equal to 3mm, the fast pyrogenation stove control is at 500~900 DEG C, institute
The temperature control at cooling tower bottom is stated at 70~90 DEG C.
8. according to the method for claim 6, it is characterised in that
In the step B, first the gas from the pyrolysis unit and the pyrolysis oil vapor treatment unit is entered on absorption tower
Row desulfurization and decarburization is reacted, and the product gas after reacting is discharged by tower top, and the desulfurization and decarburization solution for absorbing sour gas is transported to again
Raw tower, then carries out regeneration treatment to desulfurization and decarburization solution in the regenerator, the solvent after regeneration is transported into the absorption
Tower recycles, and the regenerator tower overhead gas transports to the sulphur recovery unit；
In the step C, first self-loopa recovery process is utilized using Complexing Iron sulphur as recovery solution in sulfur recovery facility
The hydrogen sulfide in sour gas is reclaimed, and the hydrogen sulfide is changed into elemental sulfur and discharged by bottom of towe, then bottom of towe arranged in baker
The elemental sulfur gone out is dried to obtain elemental sulfur.
9. according to the method for claim 6, it is characterised in that
In the step D, first using iron oxide as adsorbent in adsorption tower, the gas for coming from the pyrolysis unit is carried out
Absorption, obtains product gas；Then the adsorbent after adsorption saturation is crushed in pulverizer, the adsorbent after crushing is made
The pyrolysis oil vapor treatment unit is transported to for catalyst.
10. according to the method for claim 6, it is characterised in that
In the step E, hydrogen, catalyst and coal tar are first subjected to pre-hydrotreating, the gas that will be obtained in suspension bed
Transported to from tower top discharge and carry hydrogen production device, obtained oil product is transported to filter and filtered, and filters and makees with caused solids product
The filter is discharged for outer whipping slag；
Then hydrofinishing and hydrocracking reaction are carried out to the oil product after filtering in fixed bed, the liquid phase after reaction is produced
Product transport to gas-liquid separator；
Subsequently reacted liquid phase product is separated in the gas-liquid separator, obtained liquid phase is light-end products
Product, obtained gas, which is transported to, described carries hydrogen production device；
Finally it is described carry hydrogen production device to gas treatment after, obtained hydrogen is transported into the suspension bed and recycled, is obtained
Sour gas is transported to the desulfurization and decarburization unit and further handled；
The catalyst accounts for the 1~5% of the coal tar oil quality, the volume ratio of the hydrogen and the coal tar for 800~
2000:1。
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| 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 |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102391886A (en) * | 2011-09-27 | 2012-03-28 | 长安大学 | Dry distillation and liquefying method for coal |
| CN103265971A (en) * | 2013-05-15 | 2013-08-28 | 煤炭科学研究总院 | Heterogeneous coal tar suspension bed hydrogenation method |
| CN103509571A (en) * | 2013-09-13 | 2014-01-15 | 陕西煤业化工集团神木天元化工有限公司 | Separate utilization technology of powdered coal through combined dry distillation pyrolysis and delay coking |
| WO2015076992A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for pyrolysis of coal |
| CN104893748A (en) * | 2015-06-16 | 2015-09-09 | 西安元创化工科技股份有限公司 | Method for producing tar and hydrocarbon fuel products from coal |
| CN205133505U (en) * | 2015-10-15 | 2016-04-06 | 上海锅炉厂有限公司 | Low order coal grading utilizes many cogeneration system |
| CN206279155U (en) * | 2016-10-14 | 2017-06-27 | 北京神雾环境能源科技集团股份有限公司 | A kind of system of utilization low-order coal |
-
2016
- 2016-10-14 CN CN201610899948.4A patent/CN106318430B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102391886A (en) * | 2011-09-27 | 2012-03-28 | 长安大学 | Dry distillation and liquefying method for coal |
| CN103265971A (en) * | 2013-05-15 | 2013-08-28 | 煤炭科学研究总院 | Heterogeneous coal tar suspension bed hydrogenation method |
| CN103509571A (en) * | 2013-09-13 | 2014-01-15 | 陕西煤业化工集团神木天元化工有限公司 | Separate utilization technology of powdered coal through combined dry distillation pyrolysis and delay coking |
| WO2015076992A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for pyrolysis of coal |
| CN104893748A (en) * | 2015-06-16 | 2015-09-09 | 西安元创化工科技股份有限公司 | Method for producing tar and hydrocarbon fuel products from coal |
| CN205133505U (en) * | 2015-10-15 | 2016-04-06 | 上海锅炉厂有限公司 | Low order coal grading utilizes many cogeneration system |
| CN206279155U (en) * | 2016-10-14 | 2017-06-27 | 北京神雾环境能源科技集团股份有限公司 | A kind of system of utilization low-order coal |
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