CN106318430A - System and method utilizing low-rank coal - Google Patents
System and method utilizing low-rank coal Download PDFInfo
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- CN106318430A CN106318430A CN201610899948.4A CN201610899948A CN106318430A CN 106318430 A CN106318430 A CN 106318430A CN 201610899948 A CN201610899948 A CN 201610899948A CN 106318430 A CN106318430 A CN 106318430A
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- decarburization
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- 238000000034 method Methods 0.000 title claims abstract description 66
- 239000003245 coal Substances 0.000 title claims abstract description 65
- 239000007789 gas Substances 0.000 claims abstract description 225
- 238000000197 pyrolysis Methods 0.000 claims abstract description 147
- 235000019198 oils Nutrition 0.000 claims abstract description 123
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 100
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 80
- 238000001816 cooling Methods 0.000 claims abstract description 66
- 239000001257 hydrogen Substances 0.000 claims abstract description 66
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 66
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 64
- 238000005261 decarburization Methods 0.000 claims abstract description 62
- 239000011280 coal tar Substances 0.000 claims abstract description 61
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 239000003463 adsorbent Substances 0.000 claims abstract description 36
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 238000001914 filtration Methods 0.000 claims abstract description 26
- 238000001179 sorption measurement Methods 0.000 claims abstract description 23
- 235000019476 oil-water mixture Nutrition 0.000 claims abstract description 21
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 17
- 239000011593 sulfur Substances 0.000 claims abstract description 16
- 239000002817 coal dust Substances 0.000 claims abstract description 11
- 239000000047 product Substances 0.000 claims description 107
- 230000023556 desulfurization Effects 0.000 claims description 65
- 238000011084 recovery Methods 0.000 claims description 61
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 48
- 230000008569 process Effects 0.000 claims description 43
- 238000010521 absorption reaction Methods 0.000 claims description 36
- 239000005864 Sulphur Substances 0.000 claims description 30
- 239000007791 liquid phase Substances 0.000 claims description 27
- 238000011282 treatment Methods 0.000 claims description 26
- 239000000725 suspension Substances 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 21
- 150000002431 hydrogen Chemical class 0.000 claims description 17
- 230000032258 transport Effects 0.000 claims description 17
- 229920006395 saturated elastomer Polymers 0.000 claims description 16
- 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
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 10
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 9
- 230000000536 complexating effect Effects 0.000 claims description 9
- 239000002893 slag Substances 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 5
- 238000010298 pulverizing process Methods 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 241000748712 Colias canadensis Species 0.000 claims description 2
- 102000005298 Iron-Sulfur Proteins Human genes 0.000 claims description 2
- 108010081409 Iron-Sulfur Proteins Proteins 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 239000007790 solid phase Substances 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 2
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 44
- 239000011269 tar Substances 0.000 abstract description 29
- 239000002253 acid Substances 0.000 abstract description 6
- 238000002360 preparation method Methods 0.000 abstract description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 86
- 238000007667 floating Methods 0.000 description 10
- 239000008246 gaseous mixture Substances 0.000 description 8
- 238000007599 discharging Methods 0.000 description 6
- 239000000203 mixture Substances 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
- 238000002156 mixing Methods 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 5
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 206010037660 Pyrexia Diseases 0.000 description 1
- 230000002411 adverse Effects 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
- 238000010924 continuous production Methods 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
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 230000008570 general process Effects 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
- 230000001172 regenerating effect Effects 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
- 238000004148 unit process Methods 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 invention discloses a system and a method utilizing low-tank coal. The system comprises a pyrolysis unit, a desulfuration and decarburization unit, a sulfur recovering unit, a catalyst preparing unit and a pyrolysis oil gas processing unit, wherein the pyrolysis unit is used for pyrolyzing low-tank coal dust, filtering and cooling pyrolyzed oil gas and separating an oil-water mixture; the desulfuration and decarburization unit is used for performing desulfuration and decarburization processing on gas to obtain a product gas; the sulfur recovering unit is used for recovering hydrogen sulfide in acid gas after desulfuration and decarburization, and hydrogen sulfide is further converted into elemental sulfur; for the catalyst preparing unit, a desulfuration adsorbent is used for adsorbing the acid gas, and the adsorbent after saturation by adsorption is used as the catalyst for the pyrolysis oil gas processing unit; and the pyrolysis oil gas processing unit is used for reaction of hydrogen, the catalyst and coal tar. The system and the method can sufficiently utilize acid gas produced during coal pyrolysis and tar hydrogenation, and can complete the preparation of a coal tar suspended bed hydrogenation pretreatment catalyst while processing the acid gas with the adsorbent.
Description
Technical field
The invention belongs to coal processing technology field, particularly to a kind of system and method utilizing low-order coal.
Background technology
The utilization of coal sub-prime is considered as the effective way that Coal Clean efficiently utilizes, Ye Shi China " 13 " Coal Chemical Industry
The direction given priority to.The sub-prime of coal utilizes and is through pyrolysis and heterogeneity in coal is first separated, including coal gas,
Tar and semicoke etc..Coal tar can produce gasoline, diesel oil by hydrogenation, and semicoke becomes low volatile, low-sulfur by pyrolysis
Cleaning fuel, replace dissipating and burn coal and reduce pollution to air.
Coal sub-prime utilization " leading " is the pyrolytic technique of coal, the tar of scale production quantities to be extracted, coal gas, and coal sub-prime utilizes
Needing scale, maximization, single set pyrolysis of coal unit scale is more and more large-scale, during the sub-prime of low-order coal utilizes, soon
Speed pyrolysis is general processes fine coal raw material, and fine coal temperature in pyrolysis oven raises fast, and the time of staying is short, it is thus achieved that coal tar toluene not
Molten thing content is higher, mainly coal ash, coal dust etc., and viscosity compared with big, many containing heavy component, heat stability is poor, belong to heavy,
The category of tar inferior, these shortcomings cause its deep processing difficulty bigger.
Prior art discloses a kind of pyrolysis of coal tar recovery method, this invention is to be returned at tar with cold tar by pyrolysis gas
Receiving in tower and carry out contact heat-exchanging, make the tar condensing in pyrolysis gas reclaim, a part of condensed tar is through heat recovery and through solid-liquid
Isolating the cooling medium as pyrolysis gas after dust, a part loops back bottom tar recovery tower, improves tar and returns at tar
Receive the flow velocity of tower bottom, prevent dust deposit from blocking recovery tower.This invention utilizes heavy tar as cooling medium, part heavy
Tar needs to remove dust through solid-liquid separation, and the dust in heavy tar is difficult to remove, it is thus achieved that a certain amount of oil being difficult by
Mud, and the follow-up deep processing difficulty of heavy tar is bigger.Additionally, the method coal-tar middle oil recovery tower upper end is equipped with filler, this section cold
But temperature is low, and pyrolysis gas may carry a small amount of heavy tar and condense at this, and long-play can block cooling tower.
Prior art also discloses a kind of method improving pyrolysis of coal low temperature tar quality, and the method is by coalite tar
Or its bottoms addition feed coal carries out copyrolysis, obtain tar and the preparation method of gaseous hydrocarbon product.Concrete grammar is
Coalite tar or its bottoms are uniformly mixed with feed coal, copyrolysis in common entrance pyrolysis oven, it is thus achieved that liquid
Product, pyrolysis gas, semicoke, product liquid is oil water mixture, obtains coalite tar after oil-water separation.Low temperature in this invention
The viscosity of coal tar or its bottoms is the biggest, and it carries out mixed uniformly mode with feed coal can make coal dust become block or mud
Shape, processes to material screening, broken etc. and brings difficulty.Additionally, pyrolysis oil gas uses water-cooled, large amount of sewage, same intermittent fever can be produced
Solve oil gas heat the most effectively to utilize.
Summary of the invention
Science and engineering at the acid tail gas that the present invention has produced during having coupled the fast pyrogenation of coal, pyrolysis oil gas disposal and being somebody's turn to do
Skill.Aiming to provide a kind of with low order fine coal fast pyrogenation as source, pyrolysis oil upward adverse flow of QI effect utilizes and sour gas rationally returns
The coal high-efficiency classified utilization technique that receipts process.This technique can obtain through refining coal using low-order coal as raw material production high-quality, cleaning
Liquid fuel, and pyrolytic process can be recycled and the miscellaneous element such as S, N that petroleum resources cleans in processing procedure, accomplish
Environmental friendliness, output resource rational utilization.
For achieving the above object, the present invention proposes a kind of system utilizing low-order coal, including pyrolysis unit, desulfurization and decarburization
Unit, sulphur recovery unit, catalyst prepare unit and pyrolysis oil gas disposal unit；Wherein,
Described pyrolysis unit includes low order coal powder entrance, obtains through refining coal export, the first pyrolysis gas outlet, the second pyrolysis gas
Coal tar outlet after outlet and oil-water separation, described pyrolysis unit is for pyrolysis, pyrolysis hydrocarbon filter and the cooling of low order coal dust
And the separation of oil water mixture；
Described desulfurization and decarburization unit includes gas inlet, desulfurization and decarburization solution after the first pyrolysis gas entrance, oil vapor treatment
Sour gas outlet after entrance, the first product gas outlet and desulfurization and decarburization, described desulfurization and decarburization unit is for entering sour gas
Row desulfurization and decarburization processes and obtains product gas；
Described sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet after desulfurization and decarburization, described sulfur
Recovery unit is the recovery of hydrogen sulfide in sour gas after desulfurization and decarburization, and hydrogen sulfide is further transformed to elemental sulfur；
Described catalyst is prepared unit and is included the second pyrolysis gas entrance, the second product gas outlet and catalyst outlet,
Described catalyst is prepared unit desulfuration adsorbent and is adsorbed sour gas, adsorb saturated after adsorbent be used as described heat
Solve the catalyst of oil vapor treatment unit；
Described pyrolysis oil gas disposal unit includes coal tar entrance, hydrogen inlet after oil-water separation, catalyst inlet, lightweight
Offgas outlet after oil product product exit and oil vapor treatment, described pyrolysis oil gas disposal unit is 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 described desulfurization and decarburization unit continue
Continuous process；
Described first pyrolysis gas outlet be connected with described first pyrolysis gas entrance, described second pyrolysis gas export with
Described second pyrolysis gas entrance is connected, and after described oil-water separation, coal tar exports and coal tar entrance phase after described oil-water separation
Even, after described oil vapor treatment, gas inlet is connected with offgas outlet after described oil vapor treatment, sour gas after described desulfurization and decarburization
Outlet is connected with sour gas entrance after described desulfurization and decarburization, and catalyst outlet described in described catalyst inlet is connected.
Specifically, described pyrolysis unit is connected with splitter box order by fast pyrogenation stove, separator, cooling tower:
Described fast pyrogenation stove is for the pyrolysis of low order coal dust；
Described separator is for being pyrolyzed gas phase liquid phase and the separation of solid phase in oil gas；
Described pyrolysis oil gas after filtering used for cooling tower cools down, and obtains pyrolysis gas and enters described desulfurization and decarburization
Unit, the oil water mixture obtained enters described splitter box；
Described splitter box, for being separated by the oil water mixture after cooling, obtains the coal tar after oil-water separation and enters
Described pyrolysis oil gas disposal unit.
Further, described desulfurization and decarburization unit includes absorption tower and regenerator:
Described absorption tower is for carrying out desulfurization from the gas of described pyrolysis unit and described pyrolysis oil gas disposal unit
Decarburizing reaction, the desulfurization and decarburization solution absorbing sour gas enters described regenerator；
Described regenerator carries out Regeneration Treatment to the described desulfurization and decarburization solution absorbing sour gas, molten after regeneration
Agent returns to absorption tower and recycles, and regenerator tower overhead gas enters described sulphur recovery unit.
Further, described sulphur recovery unit includes sulfur recovery facility and baker:
Described sulfur recovery facility 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 the bottom of tower；
Described baker is for being dried the elemental sulfur discharged at the bottom of tower.
Specifically, described catalyst is prepared unit and is included adsorption tower and pulverizer:
Described adsorption tower is with ferrum oxide as adsorbent, for inhaling the sour gas coming from described pyrolysis unit
Attached；
Described pulverizer, for pulverizing absorption adsorbent after saturated, enters described as catalyst after pulverizing
Pyrolysis oil gas disposal unit.
Further, described pyrolysis oil gas disposal unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries
Hydrogen production device:
Described suspension bed is for carrying out pre-hydrotreating by hydrogen, catalyst and coal tar, and the gas obtained is arranged from tower top
Going out and carry hydrogen production device described in entering, the oil product obtained enters described filter；
Described filter, for being filtered by the oil product obtained after pre-hydrotreating, filters the solids product of generation simultaneously
As outer whipping slag discharge filter；
Described fixed bed, for the oil product from described filter is carried out hydrofinishing and hydrocracking reaction, reacts it
After liquid phase product enter described gas-liquid separator；
Described gas-liquid separator is for separating reacted liquid phase product, and the liquid phase obtained is as light-end products
Product, the gas obtained enter described in carry hydrogen production device；
The described hydrogen obtained after process gases at hydrogen production device that carries enters the recycling of described suspension bed, the sour gas obtained
Enter described desulfurization and decarburization unit.
The present invention also provides for a kind of method utilizing low-order coal, comprises the steps:
A. pyrolysis: first low order coal dust is pyrolyzed at described pyrolysis unit, then the pyrolysis oil gas obtained was carried out
Filter and cooling, obtain pyrolysis gas and oil water mixture, finally separated by described oil water mixture；
B. desulfurization and decarburization: at described desulfurization and decarburization unit, sour gas is carried out desulfurization and decarburization process and obtain product gas and take off
Sour gas after sulfur decarburization；
C. sulphur recovery: sour gas carries out hydrogen sulfide recovery after described sulphur recovery unit is to described desulfurization and decarburization,
Described hydrogen sulfide is changed into elemental sulfur；
D. prepared by catalyst: prepares unit desulfuration adsorbent at described catalyst and adsorbs sour gas, will inhale
Attached saturated after adsorbent be used as described pyrolysis oil gas disposal unit catalyst；
E. pyrolysis oil gas disposal: carry out the reaction of hydrogen, catalyst and coal tar at described pyrolysis oil gas disposal unit,
Tail gas after light-end products product and oil vapor treatment, transports to tail gas after described oil vapor treatment at described desulfurization and decarburization unit continuation
Reason.
Further, in described step A, first low order coal dust is placed in described fast pyrogenation stove and is pyrolyzed, be pyrolyzed it
After the coal of obtaining through refining that obtains discharged by furnace bottom, obtain described pyrolysis oil gas after pyrolysis and transport to described separator and gas-liquid-solid is carried out point
From；
Then the pyrolysis oil gas after described cooling tower will filter cools down, and obtains described pyrolysis gas and transports to described de-
Sulfur decarburization unit, described splitter box transported to by the described oil water mixture obtained；
Finally at described splitter box, the described oil water mixture after cooling is separated, obtain the coal tar after oil-water separation
Described pyrolysis oil gas disposal unit transported to by oil.
Preferably, by the size controlling of described low order fine coal less than or equal to 3mm, described fast pyrogenation stove controls
500～900 DEG C, the temperature at the bottom of described cooling tower controls at 70～90 DEG C.
Specifically, in described step B, first will be from described pyrolysis unit and described pyrolysis oil gas on described absorption tower
The gas of reason unit carries out desulfurization and decarburization reaction, and the product gas after reaction is discharged by tower top, absorbs the desulfurization of sour gas
Decarbonizing solution transports to described regenerator, then at described regenerator, desulfurization and decarburization solution is carried out Regeneration Treatment, after regenerating
Solvent transport to absorption tower recycle, regenerator tower overhead gas transports to described sulphur recovery unit.
Further, in described step C, first at described sulfur recovery facility using Complexing Iron sulfur as reclaiming solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, described hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower, so
After the elemental sulfur discharged at the bottom of described baker is by tower be dried and obtain elemental sulfur.
Specifically, in described step D, first with ferrum oxide as adsorbent in described adsorption tower, to coming from described heat
The gas solving unit adsorbs, and obtains product gas；Then described pulverizer by absorption saturated after adsorbent carry out powder
Broken, the adsorbent after pulverizing transports to described pyrolysis oil gas disposal unit as catalyst.
Further, in described step E, first at described suspension bed, hydrogen, catalyst and coal tar are carried out pre-hydrogenation
Processing, discharged from tower top by the gas obtained and carry hydrogen production device described in transporting to, the oil product obtained is transported to described filter and is filtered,
Filter the solids product simultaneously produced as outer whipping slag discharge filter；
Then in described fixed bed, the oil product after filtering is carried out hydrofinishing and hydrocracking reaction, after reaction
Liquid phase product transports to described gas-liquid separator；
Subsequently separating reacted liquid phase product at described gas-liquid separator, the liquid phase obtained is lightweight
Oil product product, the gas obtained transport to described in carry hydrogen production device；
Finally carry hydrogen production device to gas treatment after, the hydrogen obtained is transported to described suspension bed and recycles, obtain
Sour gas is transported to described desulfurization and decarburization unit and is processed further.
Preferably, described catalyst accounts for the volume of the 1～5% of described coal tar quality, described hydrogen and described coal tar
Ratio is 800～2000:1.
The present invention can make full use of pyrolysis of coal process and the sour gas of hydrogenation of tar process generation, and passes through adsorbent
The preparation of coal tar suspension bed hydrogenation pretreatment catalyst is completed while processing sour gas.Additionally, the present invention can
Acid tail gas produced by pyrolysis of coal, floating bed hydrogenation, oil refinery is uniformly processed, recycles.
The additional aspect of the present invention and advantage will part be given in the following description, and part will become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Accompanying drawing explanation
Fig. 1 is that the low-order coal of the present invention utilizes system structure schematic diagram.
Fig. 2 is that the low-order coal of the present invention utilizes process chart.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and various aspects thereof.But, specific embodiments described below and enforcement
Example is only descriptive purpose rather than limitation of the present invention.
The present invention is that fine coal carries out obtaining through refining process by fast pyrogenation stove, and solid product is that product obtains through refining coal, is pyrolyzed oil gas
By cooling, gaseous products enters cleaning system after electrically trapped tar oil device processes, and produces pure pyrolysis gas and enters downstream
Process technique.Pyrolytic tar carries out just hydrotreating through suspension bed, and light components enters fixed bed deep processing and produces difference
The various distillate fuel oils of fraction.
Low-order coal of the present invention processes technique, mainly comprises the steps that
(1) fine coal enters down-flow fluidized bed using ECT pyrolysis oven, and it is laggard that the pyrolysis oil gas removing dust device of generation removes bulky grain mechanical admixture
Enter chilling tower, chilling tower carry out spraying cooling,
(2) partial thermal decomposition gas entrance cleaning system carries out purified treatment, the wherein H of the pyrolysis after process2S and CO2Reach to produce
Product gas requirement, sour gas enters sulphur recovery unit, carries out sulphur recovery process；Partial thermal decomposition gas is removed by iron oxide process
Sour gas therein；
(3) coal tar that cooling is reclaimed enters suspended-bed reactor after processed, carries out pre-hydrogenation lighting
Process；
(4) oil product after processing enters after filtration treatment, fixed bed hydrogenation refining reaction and be hydrocracked instead
Answer device, produce the product oil of different fractions；
(5) gas after fixed bed hydrogenation processes is after proposing hydrogen process, and sour gas is directly entered sulphur recovery
Unit processes；
(6) iron oxide process processes containing H2Iron sulfide is converted to after pulverizing as catalyst after the sour gas of S
Participate in coal tar hydrogenating lighting reaction.
Such as Fig. 2, low-order coal of the present invention utilizes process to include following unit and process, and unit includes: fast
Speed 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 at down-flow fluidized bed using ECT, and pyrolysis oil gas mixture is discharged by the air vent of down-flow fluidized bed using ECT upper end, passes through
After pyrolysis, low order fine coal is changed into and obtains through refining coal, fast pyrogenation stove bottom discharge as product；
The pyrolysis oil gas discharged from fast pyrogenation furnace upper end enters cooling tower after filtering, and is pyrolyzed oil gas in cooling tower
Entering from cooling tower lower end tower, cooling water enters tower with pyrolysis oil QI rising in reverse order to contacting cooling from upper end, the most cooled gas
Discharging cooling tower from tower top, the oil water mixture after cooling is flowed out by the bottom of tower；
Pyrolysis gas and process carry after the partial hydrogenation reaction end gas after hydrogen processes mixes by there being lower end, absorption tower to enter,
Desulfurization solvent is flowed into absorption tower by tower top, contact with back flow of gas carry out remove acidic components react, the product gas after reaction
Being discharged by tower top, the desulfuration solution absorbing sour gas enters regenerator；
Entered by adsorption tower upper end, only after pyrolysis gas and the partial hydrogenation reaction end gas mixing after proposing hydrogen process
Gas after change is discharged into product gas pipeline by tower bottom；
Absorbing the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Using, regenerator tower overhead gas is discharged into next unit；
Regenerator tower top sour gas enters sulphur recovery unit, and sulphur recovery unit uses Complexing Iron sulphur recovery solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower；
Desulfuration adsorbent (ferrum oxide) after adsorption tower internal adsorption is saturated, enters pulverizer after discharging at the bottom of tower and carries out powder
Suspension bed is entered as catalyst after broken；
Entered surge tank by the mixture of the coal tar after the cooling discharged at the bottom of cooling tower and water, carry out oil-water separation, point
Floating bed hydrogenation unit is entered from coal tar afterwards；
Hydrogen, catalyst enter suspension bed together with coal tar and carry out pre-hydrotreating, and the gas after hydrogenation is from suspension
Bed tower top is discharged, and the oil product after pre-hydrotreating enters next unit after filtering；
The pre-oil product that is hydrogenated with is after filtering, and liquid-phase product enters fixed bed hydrogenation unit, filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre-hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters carry hydrogen production device, hydrogen as light-end products product, gas
Can recycle, tail gas enters absorption tower.
Tail gas produced during pyrolysis of coal process and coal tar hydrogenating is utilized by the present invention in batches, is processing sour gas
On the basis of body again enable to process after adsorbent as the catalyst of coal tar suspension bed pre-hydrotreating, reach
The effect of comprehensive utilization and purpose.
Below with reference to specific embodiment, present invention is described, it should be noted that these embodiments are only to describe
Property, and limit the present invention never in any form.
Embodiment 1
The present embodiment proposes a kind of system processing coal tar, including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery
Unit, catalyst prepare unit and pyrolysis oil gas disposal unit:
Low order fine coal particle diameter (≤3mm), is pyrolyzed at down-flow fluidized bed using ECT, and it is 700 DEG C that lower formation temperature controls, and pyrolysis oil gas mixes
Compound is discharged by the air vent of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
The pyrolysis oil gas discharged from fast pyrogenation furnace upper end enters cooling tower after filtering, and is pyrolyzed oil gas in cooling tower
Entering from cooling tower lower end tower, cooling water enters tower with pyrolysis oil QI rising in reverse order to contacting cooling from upper end, tower after cooling processes
The temperature at the end controls at 80 DEG C, and the most cooled gas discharges cooling tower from tower top, and the oil water mixture after cooling is at the bottom of by tower
Flow out；
The pyrolysis gas entered by lower end, absorption tower and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
Amount 99.5%, desulfurization solvent is flowed into absorption tower by tower top, contact with back flow of gas carry out removing acidic components react, react it
After product gas discharged the sulfur content≤20ppm, CO in product gas by tower top2≤ 2%, absorb the desulfuration solution of sour gas
Enter regenerator；
The pyrolysis gas entered by adsorption tower top and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
The 0.5% of amount, the gas after purifying is discharged at the bottom of by tower, enters product gas pipeline；
Absorbing the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Using, regenerator tower overhead gas is discharged into next unit；
Regenerator tower top sour gas enters sulphur recovery unit, and sulphur recovery unit uses Complexing Iron sulphur recovery solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower；
Adsorbent after the adsorption of hydrogen sulfide of discharge is saturated in adsorption tower, with hydrogen, coal tar after pulverizer is pulverized
Entering floating bed hydrogenation reactor after oil mixing, the mass ratio of the adsorbent and coal tar that enter this unit is 3:100；
Entered surge tank by the mixture of the coal tar after the cooling discharged at the bottom of cooling tower and water, carry out oil-water separation, point
Floating bed hydrogenation unit is entered from coal tar afterwards；
Hydrogen, catalyst (adsorbing saturated adsorbent) enter suspension bed together with coal tar and carry out pre-hydrotreating, urge
Agent accounts for the 2% of tar stock quality, and hydrogen is 1200:1 with the volume ratio of tar.Gas after hydrogenation is from suspension bed tower top
Discharging, the oil product after pre-hydrotreating enters next unit after filtering；
The pre-oil product that is hydrogenated with is after filtering, and liquid-phase product enters fixed bed hydrogenation unit, filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre-hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters carry hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Embodiment 2
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed at down-flow fluidized bed using ECT, and it is 500 DEG C that lower formation temperature controls, and pyrolysis oil gas mixes
Compound is discharged by the air vent of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
The pyrolysis oil gas discharged from fast pyrogenation furnace upper end enters cooling tower after filtering, and is pyrolyzed oil gas in cooling tower
Entering from cooling tower lower end tower, cooling water enters tower with pyrolysis oil QI rising in reverse order to contacting cooling from upper end, tower after cooling processes
The temperature at the end controls at 70 DEG C, and the most cooled gas discharges cooling tower from tower top, and the oil water mixture after cooling is at the bottom of by tower
Flow out；
The pyrolysis gas entered by lower end, absorption tower and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
Amount 99.5%, desulfurization solvent is flowed into absorption tower by tower top, contact with back flow of gas carry out removing acidic components react, react it
After product gas discharged the sulfur content≤20ppm, CO in product gas by tower top2≤ 2%, absorb the desulfuration solution of sour gas
Enter regenerator；
The pyrolysis gas entered by adsorption tower top and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
The 0.5% of amount, the gas after purifying is discharged at the bottom of by tower, enters product gas pipeline；
Absorbing the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Using, regenerator tower overhead gas is discharged into next unit；
Regenerator tower top sour gas enters sulphur recovery unit, and sulphur recovery unit uses Complexing Iron sulphur recovery solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower；
Adsorbent after the adsorption of hydrogen sulfide of discharge is saturated in adsorption tower, with hydrogen, coal tar after pulverizer is pulverized
Entering floating bed hydrogenation reactor after oil mixing, the mass ratio of the adsorbent and coal tar that enter this unit is 3:100；
Entered surge tank by the mixture of the coal tar after the cooling discharged at the bottom of cooling tower and water, carry out oil-water separation, point
Floating bed hydrogenation unit is entered from coal tar afterwards；
Hydrogen, catalyst (adsorbing saturated adsorbent) enter suspension bed together with coal tar and carry out pre-hydrotreating, urge
Agent accounts for the 4% of tar stock quality, and hydrogen is 1500:1 with the volume ratio of tar.Gas after hydrogenation is from suspension bed tower top
Discharging, the oil product after pre-hydrotreating enters next unit after filtering；
The pre-oil product that is hydrogenated with is after filtering, and liquid-phase product enters fixed bed hydrogenation unit, filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre-hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters carry hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Embodiment 3
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed at down-flow fluidized bed using ECT, and it is 900 DEG C that lower formation temperature controls, and pyrolysis oil gas mixes
Compound is discharged by the air vent of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
The pyrolysis oil gas discharged from fast pyrogenation furnace upper end enters cooling tower after filtering, and is pyrolyzed oil gas in cooling tower
Entering from cooling tower lower end tower, cooling water enters tower with pyrolysis oil QI rising in reverse order to contacting cooling from upper end, tower after cooling processes
The temperature at the end controls at 90 DEG C, and the most cooled gas discharges cooling tower from tower top, and the oil water mixture after cooling is at the bottom of by tower
Flow out；
The pyrolysis gas entered by lower end, absorption tower and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
Amount 99.5%, desulfurization solvent is flowed into absorption tower by tower top, contact with back flow of gas carry out removing acidic components react, react it
After product gas discharged the sulfur content≤20ppm, CO in product gas by tower top2≤ 2%, absorb the desulfuration solution of sour gas
Enter regenerator；
The pyrolysis gas entered by adsorption tower top and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
The 0.4% of amount, the gas after purifying is discharged at the bottom of by tower, enters product gas pipeline；
Absorbing the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Using, regenerator tower overhead gas is discharged into next unit；
Regenerator tower top sour gas enters sulphur recovery unit, and sulphur recovery unit uses Complexing Iron sulphur recovery solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower；
Adsorbent after the adsorption of hydrogen sulfide of discharge is saturated in adsorption tower, with hydrogen, coal tar after pulverizer is pulverized
Entering floating bed hydrogenation reactor after oil mixing, the mass ratio of the adsorbent and coal tar that enter this unit is 3:120；
Entered surge tank by the mixture of the coal tar after the cooling discharged at the bottom of cooling tower and water, carry out oil-water separation, point
Floating bed hydrogenation unit is entered from coal tar afterwards；
Hydrogen, catalyst (adsorbing saturated adsorbent) enter suspension bed together with coal tar and carry out pre-hydrotreating, urge
Agent accounts for the 1% of tar stock quality, and hydrogen is 2000:1 with the volume ratio of tar.Gas after hydrogenation is from suspension bed tower top
Discharging, the oil product after pre-hydrotreating enters next unit after filtering；
The pre-oil product that is hydrogenated with is after filtering, and liquid-phase product enters fixed bed hydrogenation unit, filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre-hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters carry hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Embodiment 4
The present embodiment is as above-described embodiment 1 system for use in carrying, but process conditions are different, as described below:
Low order fine coal particle diameter (≤3mm), is pyrolyzed at down-flow fluidized bed using ECT, and it is 800 DEG C that lower formation temperature controls, and pyrolysis oil gas mixes
Compound is discharged by the air vent of down-flow fluidized bed using ECT upper end, and after pyrolysis, low order fine coal is changed into and obtains through refining coal, by under fast pyrogenation stove
Portion discharges as product；
The pyrolysis oil gas discharged from fast pyrogenation furnace upper end enters cooling tower after filtering, and is pyrolyzed oil gas in cooling tower
Entering from cooling tower lower end tower, cooling water enters tower with pyrolysis oil QI rising in reverse order to contacting cooling from upper end, tower after cooling processes
The temperature at the end controls at 80 DEG C, and the most cooled gas discharges cooling tower from tower top, and the oil water mixture after cooling is at the bottom of by tower
Flow out；
The pyrolysis gas entered by lower end, absorption tower and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
Amount 99.5%, desulfurization solvent is flowed into absorption tower by tower top, contact with back flow of gas carry out removing acidic components react, react it
After product gas discharged the sulfur content≤20ppm, CO in product gas by tower top2≤ 2%, absorb the desulfuration solution of sour gas
Enter regenerator；
The pyrolysis gas entered by adsorption tower top and the hydrogenation reaction tail gas gaseous mixture after proposing hydrogen process account for total gas
The 0.6% of amount, the gas after purifying is discharged at the bottom of by tower, enters product gas pipeline；
Absorbing the desulfurization and decarburization solution of sour gas, enter regenerator, the solvent after regeneration returns absorption tower circulation
Using, regenerator tower overhead gas is discharged into next unit；
Regenerator tower top sour gas enters sulphur recovery unit, and sulphur recovery unit uses Complexing Iron sulphur recovery solution,
Utilizing self-loopa recovery process to reclaim the hydrogen sulfide in sour gas, hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower；
Adsorbent after the adsorption of hydrogen sulfide of discharge is saturated in adsorption tower, with hydrogen, coal tar after pulverizer is pulverized
Entering floating bed hydrogenation reactor after oil mixing, the mass ratio of the adsorbent and coal tar that enter this unit is 3:90；
Entered surge tank by the mixture of the coal tar after the cooling discharged at the bottom of cooling tower and water, carry out oil-water separation, point
Floating bed hydrogenation unit is entered from coal tar afterwards；
Hydrogen, catalyst (adsorbing saturated adsorbent) enter suspension bed together with coal tar and carry out pre-hydrotreating, urge
Agent accounts for the 5% of tar stock quality, and hydrogen is 800:1 with the volume ratio of tar.Gas after hydrogenation is from suspension bed tower top
Discharging, the oil product after pre-hydrotreating enters next unit after filtering；
The pre-oil product that is hydrogenated with is after filtering, and liquid-phase product enters fixed bed hydrogenation unit, filters consolidating of generation simultaneously
Phase product is as outer whipping slag discharge filter；
Pre-hydrogenated products oil after filtration enters fixed bed hydrogenation reactor and carries out hydrofinishing and hydrocracking reaction,
Liquid phase product after reaction enters gas-liquid separator, and liquid phase enters carry hydrogen production device, hydrogen as light-end products product, gas
Can recycle, sour gas enters absorption tower.
Although above it has been shown and described that embodiments of the invention, it is to be understood that above-described embodiment is example
Property, it is impossible to being interpreted as limitation of the present invention, those of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, revises, replaces and modification.
What present disclosure was touched upon is exemplary embodiment, at the protection domain defined without departing from claims
In the case of, each embodiment of the application can be made various changes and modifications.Therefore, described embodiment is intended to contain
All this type of that lid falls in the protection domain of appended claims changes, revises and deform.Additionally, institute unless the context
Outside finger, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can in conjunction with any other embodiments all or part of use.
Claims (10)
1. utilize a system for low-order coal, prepare including pyrolysis unit, desulfurization and decarburization unit, sulphur recovery unit, catalyst
Unit and pyrolysis oil gas disposal unit；Wherein,
Described pyrolysis unit includes low order coal powder entrance, obtains through refining coal export, the first pyrolysis gas outlet, the second pyrolysis gas outlet
Export with coal tar after oil-water separation, described pyrolysis unit for low order coal dust pyrolysis, pyrolysis hydrocarbon filter and cooling and
The separation of oil water mixture；
Described desulfurization and decarburization unit include gas inlet after the first pyrolysis gas entrance, oil vapor treatment, desulfurization and decarburization solution inlet,
Sour gas outlet after first product gas outlet and desulfurization and decarburization, described desulfurization and decarburization unit is for carrying out desulfurization and decarburization by gas
Process obtains product gas；
Described sulphur recovery unit includes sour gas entrance and sulphur recovery solution inlet after desulfurization and decarburization, described sulphur recovery
Unit is the recovery of hydrogen sulfide in sour gas after desulfurization and decarburization, and hydrogen sulfide is further transformed to elemental sulfur；
Described catalyst is prepared unit and is included the second pyrolysis gas entrance, the second product gas outlet and catalyst outlet, described
Catalyst is prepared unit desulfuration adsorbent and is adsorbed sour gas, adsorb saturated after adsorbent be used as described pyrolysis oil
The catalyst of gas disposal unit；
Described pyrolysis oil gas disposal unit includes coal tar entrance, hydrogen inlet after oil-water separation, catalyst inlet, light-end products
Offgas outlet after product exit and oil vapor treatment, described pyrolysis oil gas disposal unit is anti-for hydrogen, catalyst and coal tar
Should, obtaining tail gas after light-end products product and oil vapor treatment, after oil vapor treatment, tail gas enters at described desulfurization and decarburization unit continuation
Reason；
Described first pyrolysis gas outlet is connected with described first pyrolysis gas entrance, and described second pyrolysis gas outlet is with described
Second pyrolysis gas entrance is connected, and after described oil-water separation, coal tar outlet is connected with coal tar entrance after described oil-water separation,
After described oil vapor treatment, gas inlet is connected with offgas outlet after described oil vapor treatment, sour gas outlet after described desulfurization and decarburization
Being connected with sour gas entrance after described desulfurization and decarburization, catalyst outlet described in described catalyst inlet is connected.
System the most according to claim 1, it is characterised in that
Described pyrolysis unit is connected with splitter box order by fast pyrogenation stove, separator, cooling tower:
Described fast pyrogenation stove is for the pyrolysis of low order coal dust；
Described separator is for being pyrolyzed gas phase liquid phase and the separation of solid phase in oil gas；
Described pyrolysis oil gas after filtering used for cooling tower cools down, and obtains pyrolysis gas and enters described desulfurization and decarburization list
Unit, the oil water mixture obtained enters described splitter box；
Described splitter box, for being separated by the oil water mixture after cooling, obtains the coal tar after oil-water separation and enters described
Pyrolysis oil gas disposal unit.
System the most according to claim 1, it is characterised in that
Described desulfurization and decarburization unit includes absorption tower and regenerator:
Described absorption tower is for carrying out desulfurization and decarburization from the gas of described pyrolysis unit and described pyrolysis oil gas disposal unit
Reaction, the desulfurization and decarburization solution absorbing sour gas enters described regenerator；
Described regenerator carries out Regeneration Treatment to the described desulfurization and decarburization solution absorbing sour gas, and the solvent after regeneration returns
Going back to absorption tower to recycle, regenerator tower overhead gas enters described sulphur recovery unit；
Described sulphur recovery unit includes sulfur recovery facility and baker:
Described sulfur recovery facility uses Complexing Iron sulphur recovery solution, reclaims the hydrogen sulfide in sour gas, and hydrogen sulfide changes
Discharge by the bottom of tower for elemental sulfur；
Described baker is for being dried the elemental sulfur discharged at the bottom of tower.
System the most according to claim 1, it is characterised in that
Described catalyst is prepared unit and is included adsorption tower and pulverizer:
Described adsorption tower is with ferrum oxide as adsorbent, for adsorbing the sour gas coming from described pyrolysis unit；
Described pulverizer for absorption saturated after adsorbent pulverize, after pulverizing as catalyst enter described pyrolysis
Oil vapor treatment unit.
System the most according to claim 1, it is characterised in that
Described pyrolysis oil gas disposal unit includes suspension bed, filter, fixed bed, gas-liquid separator and carries hydrogen production device:
Described suspension bed for hydrogen, catalyst and coal tar are carried out pre-hydrotreating, the gas obtained from tower top discharge into
Carrying hydrogen production device described in entering, the oil product obtained enters described filter；
Described filter, for being filtered by the oil product obtained after pre-hydrotreating, filters the solids product conduct of generation simultaneously
Outer whipping slag discharge filter；
Described fixed bed is for carrying out hydrofinishing and hydrocracking reaction, after reaction by the oil product from described filter
Liquid phase product enters described gas-liquid separator；
Described gas-liquid separator is for separating reacted liquid phase product, and the liquid phase obtained is produced as light-end products
Thing, the gas obtained enter described in carry hydrogen production device；
The described hydrogen obtained after process gases at hydrogen production device that carries enters the recycling of described suspension bed, and the sour gas obtained enters
Described desulfurization and decarburization unit.
6. the method utilizing low-order coal by system described in claim 1, it is characterised in that include step:
A. pyrolysis: first low order coal dust is pyrolyzed at described pyrolysis unit, then the pyrolysis oil gas obtained is carried out filter and
Cooling, obtains pyrolysis gas and oil water mixture, is finally separated by described oil water mixture；
B. desulfurization and decarburization: at described desulfurization and decarburization unit, sour gas carried out desulfurization and decarburization and process and obtain product gas and desulfurization takes off
Sour gas after carbon；
C. sulphur recovery: sour gas carries out hydrogen sulfide recovery after described sulphur recovery unit is to described desulfurization and decarburization, described
Hydrogen sulfide is changed into elemental sulfur；
D. prepared by catalyst: prepares unit desulfuration adsorbent at described catalyst and adsorbs sour gas, absorption is satisfied
Adsorbent after with is used as the catalyst of described pyrolysis oil gas disposal unit；
E. pyrolysis oil gas disposal: carry out the reaction of hydrogen, catalyst and coal tar at described pyrolysis oil gas disposal unit, obtains light
Tail gas after matter oil product product and oil vapor treatment, transports to described desulfurization and decarburization unit by tail gas after described oil vapor treatment and continues with.
Method the most according to claim 6, it is characterised in that
In described step A, low order coal dust being first placed in described fast pyrogenation stove and is pyrolyzed, obtain after pyrolysis obtains through refining coal
Discharged by furnace bottom, obtain described pyrolysis oil gas after pyrolysis and transport to described separator gas-liquid-solid is separated；
Then described cooling tower will filter after pyrolysis oil gas cool down, obtain described pyrolysis gas transport to described desulfurization take off
Carbon unit, described splitter box transported to by the described oil water mixture obtained；
Finally at described splitter box, the described oil water mixture after cooling is separated, obtain the coal tar after oil-water separation defeated
To described pyrolysis oil gas disposal unit；
By the size controlling of described low order fine coal less than or equal to 3mm, described fast pyrogenation stove controls at 500～900 DEG C, institute
State the temperature at the bottom of cooling tower to control at 70～90 DEG C.
Method the most according to claim 6, it is characterised in that
In described step B, first on described absorption tower by from described pyrolysis unit and the gas of described pyrolysis oil gas disposal unit
Body carries out desulfurization and decarburization reaction, and the product gas after reaction is discharged by tower top, and the desulfurization and decarburization solution absorbing sour gas is defeated
To described regenerator, then at described regenerator, desulfurization and decarburization solution is carried out Regeneration Treatment, the solvent after regeneration is transported to
Absorption tower recycles, and regenerator tower overhead gas transports to described sulphur recovery unit；
In described step C, first at described sulfur recovery facility using Complexing Iron sulfur as reclaiming solution, self-loopa is utilized to reclaim
Technique reclaims the hydrogen sulfide in sour gas, and described hydrogen sulfide is changed into elemental sulfur and is discharged by the bottom of tower, then at described baker
The elemental sulfur discharged at the bottom of tower is dried and obtains elemental sulfur.
Method the most according to claim 6, it is characterised in that
In described step D, first with ferrum oxide as adsorbent in described adsorption tower, to the gas coming from described pyrolysis unit
Adsorb, obtain product gas；Then described pulverizer by absorption saturated after adsorbent pulverize, by pulverize after
Adsorbent transports to described pyrolysis oil gas disposal unit as catalyst.
Method the most according to claim 6, it is characterised in that
In described step E, first at described suspension bed, hydrogen, catalyst and coal tar are carried out pre-hydrotreating, by obtain
Gas from tower top discharge transport to described in carry hydrogen production device, the oil product obtained is transported to described filter and is filtered, filter produce simultaneously
Solids product as outer whipping slag discharge filter；
Then in described fixed bed, the oil product after filtering is carried out hydrofinishing and hydrocracking reaction, by the gas-liquid after reaction
Phase product transports to described gas-liquid separator；
Subsequently separating reacted liquid phase product at described gas-liquid separator, the liquid phase obtained is light-end products
Product, the gas obtained transport to described in carry hydrogen production device；
Finally carry hydrogen production device to gas treatment after, the hydrogen obtained is transported to described suspension bed and recycles, the acidity obtained
Gas is transported to described desulfurization and decarburization unit and is processed further；
Described catalyst accounts for the 1～5% of described coal tar quality, the volume ratio of described hydrogen and described coal tar be 800～
2000:1。
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| CN107523316A (en) * | 2017-10-17 | 2017-12-29 | 榆林煤化工产业促进中心 | A kind of hydrogen source stably decomposes complex function low temperature upgrading furnace |
| CN114479897A (en) * | 2020-11-13 | 2022-05-13 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar and method and device for preparing fuel oil from coal |
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| CN102391886A (en) * | 2011-09-27 | 2012-03-28 | 长安大学 | Dry distillation and liquefying method for coal |
| CN103265971B (en) * | 2013-05-15 | 2015-03-25 | 煤炭科学研究总院 | Heterogeneous coal tar suspension bed hydrogenation method |
| CN103509571B (en) * | 2013-09-13 | 2016-03-09 | 陕西煤业化工集团神木天元化工有限公司 | A kind of fine coal carbonization and delayed coking combination sub-prime utilize technology |
| US20150136656A1 (en) * | 2013-11-19 | 2015-05-21 | 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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| CN107523316A (en) * | 2017-10-17 | 2017-12-29 | 榆林煤化工产业促进中心 | A kind of hydrogen source stably decomposes complex function low temperature upgrading furnace |
| CN114479897A (en) * | 2020-11-13 | 2022-05-13 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar and method and device for preparing fuel oil from coal |
| CN114479897B (en) * | 2020-11-13 | 2023-05-26 | 国家能源投资集团有限责任公司 | Method and device for producing coal tar, method and device for producing fuel oil by coal |
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