CN106833704A - A kind of pyrolysis of coal production of synthetic gas system and method - Google Patents
A kind of pyrolysis of coal production of synthetic gas system and method Download PDFInfo
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- CN106833704A CN106833704A CN201710206303.2A CN201710206303A CN106833704A CN 106833704 A CN106833704 A CN 106833704A CN 201710206303 A CN201710206303 A CN 201710206303A CN 106833704 A CN106833704 A CN 106833704A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 197
- 239000003245 coal Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 238000009825 accumulation Methods 0.000 claims abstract description 52
- 239000002470 thermal conductor Substances 0.000 claims abstract description 26
- 239000007789 gas Substances 0.000 claims description 133
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 32
- 239000000463 material Substances 0.000 claims description 30
- 239000007921 spray Substances 0.000 claims description 26
- 239000003546 flue gas Substances 0.000 claims description 25
- 238000001035 drying Methods 0.000 claims description 23
- 230000015572 biosynthetic process Effects 0.000 claims description 20
- 238000003786 synthesis reaction Methods 0.000 claims description 20
- 239000007787 solid Substances 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- 239000000446 fuel Substances 0.000 claims description 12
- 238000011068 loading method Methods 0.000 claims description 12
- 239000000567 combustion gas Substances 0.000 claims description 11
- 239000011148 porous material Substances 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 7
- 238000004939 coking Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 238000005299 abrasion Methods 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 239000007769 metal material Substances 0.000 claims description 3
- 230000026676 system process Effects 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000003077 lignite Substances 0.000 description 3
- 239000000969 carrier Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 230000010512 thermal transition Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/20—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge according to the moving bed type
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The present invention proposes a kind of pyrolysis of coal production of synthetic gas system and method, and the system includes：Pyrolysis hopper；First feed arrangement, the first feed arrangement is connected with the pyrolysis hopper；Pyrolysis reactor, including：Charging aperture, pyrolysis gas outlet, multiple pyrolysis chambers and multiple radiant tube rooms, charging aperture is arranged on the roof of each pyrolysis chamber, pyrolysis hopper is connected by the first feed arrangement with charging aperture, and pyrolysis gas outlet is arranged on the side wall of each radiant tube room and each pyrolysis chamber, and：Thermal conductor, the thermal conductor along the reactor laterally have be positioned apart from, and vertically through in reactor, the inner space of reactor is separated into the multiple chambers as multiple pyrolysis chambers and multiple radiant tube rooms, and pyrolysis chamber and radiant tube room are arranged alternately；Heat accumulation type radiant tube, along the short transverse multi-tier arrangement of reactor in radiant tube chamber interior, the system process is simple, and the thermal efficiency is high for heat accumulation type radiant tube, low cost and simple to operate.
Description
Technical field
The invention belongs to pyrolysis of coal aerogenesis technical field, it is mainly based upon heat accumulation type radiant tube and heats pyrolysis of coal system to make
Take synthesis gas system, and in particular to a kind of pyrolysis of coal production of synthetic gas system and method.
Background technology
Rich coal resources in China, in addition to part is used for coking, conversion processing, the overwhelming majority is for directly firing for raw coal
Burn.Coal directly burns, and causes the petroleum resources being rich in coal not obtain also sufficiently refining utilization, and the directly combustion heat
Efficiency is low, serious to environmental disruption.The pyrolysis of coal is to heat coal under an inert atmosphere, produces the product such as semicoke, coal gas and tar
Product, these products for obtaining can again improve the synthesis of coal with cascade utilization, while fully extraction to petroleum resources again
Utilization ratio.Pyrolytic process of coal can be divided into external-heat and the class of internal heat type two.External heating type heat efficiency is low, and volatility product twice decomposition is tight
Weight；Internal heat type technique overcomes the shortcoming of external-heat, by heat carrier（Solid thermal carriers and gas heat carrier）Heat transfer
To coal., there are carbonization gas and rushed dilute in gas heat carrier technique, condensate recovery system is huge, and gas heating value is low, it is difficult to further comprehensive
The shortcoming that conjunction is utilized.Comparatively solid thermal carriers technique have certain advantage, but there is complex process operation link too
It is many, the shortcomings of manufacturing cost is high.Therefore, a kind of process is simple, efficiency high and pyrolysis of coal with low cost how to be designed and produces conjunction
Turn into the technical problem of this area urgent need to resolve into gas system.
The content of the invention
The present invention is in view of the shortcomings of the prior art, it is proposed that a kind of pyrolysis of coal production of synthetic gas system and method, the system work
Skill is simple, and the thermal efficiency is high, low cost and simple to operate.
In order to solve the above technical problems, the technical scheme that the present invention takes is：The present invention proposes a kind of pyrolysis of coal and produces conjunction
Into gas system, it is characterised in that including：Pyrolysis hopper；First feed arrangement, first feed arrangement and the pyrolysis hopper
Connection；Pyrolysis reactor, including：Charging aperture, pyrolysis gas outlet, multiple pyrolysis chambers and multiple radiant tube rooms, the charging aperture set
Put on the roof of each pyrolysis chamber, the pyrolysis hopper is connected by first feed arrangement with the charging aperture,
The pyrolysis gas outlet is arranged on the side wall of described each radiant tube room and each pyrolysis chamber, and：Thermal conductor, the heat transfer
Body laterally has along the reactor and is positioned apart from, and vertically through in the reactor, by the reactor
Portion space is separated into the multiple chambers as the multiple pyrolysis chamber and multiple radiant tube rooms, and the pyrolysis chamber and radiant tube room
It is arranged alternately；Heat accumulation type radiant tube, the heat accumulation type radiant tube is along the short transverse multi-tier arrangement of the reactor in the spoke
Penetrate pipe chamber interior, the thermal conductor makes the charging in the heat accumulation type radiant tube of the radiant tube chamber interior and the pyrolysis chamber
It is separated, pyrolysis processing is carried out to the material in pyrolysis chamber using radiant heat, prevents the heat accumulation type radiant tube coking and mill
Damage；Spray column, the spray column is connected with the pyrolysis gas outlet；Tar tank, the tar tank is connected with the spray column；Turn
Change stove, the reburner is connected with the spray column；Fuel cartridge, the fuel cartridge is connected with the reburner.
Further, multiple pore areas are provided with the thermal conductor, the aperture of the pore area is 3-30mm, its total perforate face
Product accounts for the 20-60% of the thermal conductor gross area.
Further, further include：Combustion gas air-introduced machine, one end of the combustion gas air-introduced machine and the outlet of the spray column
It is connected, the other end is connected with the import of the reburner.
Further, also include：Loading hopper；Second feed arrangement, it is connected with the loading hopper；Drying device, its point
It is not connected with the exhanst gas outlet on second feed arrangement and the heat accumulation type radiant tube；Gas-solid separating device, its respectively with
The drying device is connected with the pyrolysis hopper；Exhaust gas cleaner, it passes through tail gas air-introduced machine with the gas solid separation
Device is connected；Chimney, the chimney is connected with the exhaust gas cleaner.
Further, further include that semicoke is exported, the semicoke outlet is arranged on described each pyrolysis chamber and each spoke
The bottom of pipe room is penetrated, the semicoke outlet is connected with semicoke conveying device.
Further, the thermal conductor is the metal material that readily conducts heat, and first feed arrangement is rotary feeder.
In another aspect of this invention, there is provided a kind of to carry out pyrolysis of coal product conjunction using above-mentioned pyrolysis of coal production of synthetic gas system
Into the method for gas, it is characterised in that comprise the following steps：A. particulate coal is entered into drying device by loading hopper, by pyrolysis
The flue gas of the heat accumulation type radiant tube smoke outlet of reactor is dried and is lifted to coal, then into gas solid separation dress
Put, the coal of separation by being pyrolyzed hopper through the charging aperture into being pyrolyzed in the pyrolysis chamber of the reactor, the cigarette of separation
Gas enters exhaust gas cleaner through tail gas air-introduced machine, and the flue gas after purification is discharged through chimney；B. the coal for separate is in described each warm
Solution stays for some time from top to bottom in room, is radiated by the heat accumulating type for separating the radiant tube chamber interior for setting with the pyrolysis chamber
Pipe carries out high temperature pyrolysis, completes pyrolytic process, while the flue gas for producing is gone out by the heat accumulation type radiant tube flue gas of pyrolysis reactor
Mouth enters drying device, recycles；C. the oil gas of generation is pyrolyzed by the radiant tube room and the pyrolysis gas outlet of pyrolysis chamber
Condensed into spray column and purified treatment, be pyrolyzed the semicoke for producing through the pyrolysis chamber and the semicoke of radiant tube room bottom
Outlet is discharged into the semicoke conveying device；D. the cold oil after condensed enters in tar tank and stores, it is purified after
Not coagulate pyrolysis gas enter reburner through combustion gas pressure fan, in the reburner, coagulate pyrolysis gas be converted into synthesis gas；E. institute
Synthesis gas is stated to be stored into fuel cartridge.
Further, in the step b, the high-temperature temperature is 500-600 DEG C, and the residence time is 10-100min；
In the step a and step b, the flue-gas temperature of the radiant tube smoke outlet is 150-250 DEG C.
Further, in the step d, the pyrolysis gas that do not coagulate include：Methane and many carbon appropriate hydrocarbon gas；The step d and
In step e, the synthesis gas is carbon monoxide and Hydrogen synthesis gas.
Further, the granularity of the particulate coal is below 20mm.
The present invention at least includes following beneficial effect：
1）Heat accumulation type radiant tube moving bed pyrolysis reactor is taken to heat the coal charge of below 20mm, uniformity of temperature profile, heating effect
Really good, reaction system simple structure is easy to operate；
2）Pyrolysis gas are not diluted, and pyrolysis gas calorific value is high；
3）Pyrolysis reactor is vertical heater, and simple structure saves construction cost and floor space；
4）Set thermal conductor the inner space of the reactor is separated into as the multiple pyrolysis chamber and multiple radiant tube rooms
Multiple chambers, and the pyrolysis chamber and radiant tube room be arranged alternately, and in the case of fully pyrolysis, the thermal conductor makes described
Charging in the heat accumulation type radiant tube of radiant tube chamber interior and the pyrolysis chamber is separated, using radiant heat to pyrolysis chamber
Interior material carries out pyrolysis processing, effectively prevent material and is contacted with heat accumulation type radiant tube, prevents heat accumulation type radiant tube from wearing and tearing, tying
Jiao, extends the service life of heat accumulation type radiant tube, improves system operation reliability；
5）Pyrolysis gas enter in reburner, can be carbon monoxide and hydrogen by methane and a small number of many carbon gaseous hydrocarbons, synthesize many
Plant product.
Brief description of the drawings
Fig. 1 is the structural representation of pyrolysis of coal production of synthetic gas system of the present invention.
Wherein, 1. loading hopper；101. second feed arrangements；2. riser drier；3. thermal storage type moving bed pyrolytic reaction
Device；301. pyrolysis chambers；302. radiant tube rooms；303. thermal conductors；304. charging apertures；305. pyrolysis gas outlets；306. heat accumulating type spokes
Penetrate pipe；307. exhanst gas outlets；308. air intakes；309. semicokes are exported；4. cyclone separator is dried；5. hopper is pyrolyzed；6. tail
Gas air-introduced machine；7. exhaust gas cleaner；8. chimney；9. rotary feeder；10. spray column；11. tar tanks；12. combustion gas air inducing
Machine；13. reburners；14. conveying worms；15. fuel cartridges.
Specific embodiment
In order that those skilled in the art more fully understand technical scheme, with reference to specific embodiment to this
Invention is described in further detail.The embodiments described below is exemplary, is only used for explaining the present invention, without being understood that
It is limitation of the present invention.Unreceipted particular technique or condition in embodiment, according to the skill described by document in the art
Art or condition are carried out according to product description.
Embodiments in accordance with the present invention, the present invention proposes a kind of pyrolysis of coal production of synthetic gas system, and Fig. 1 is coal of the present invention heat
The structural representation of production of synthetic gas system is solved, shown in reference picture 1, the system includes：Pyrolysis hopper 5, the first feed arrangement, pyrolysis
Reactor 3, thermal conductor 303, heat accumulation type radiant tube 306, spray column 10, tar tank 11, reburner 13, fuel cartridge 15, combustion gas draw
Blower fan 12, loading hopper 1, the second feed arrangement 101, drying device, gas-solid separating device, exhaust gas cleaner 7, chimney 8 and half
Burnt conveying device.
Inventor has found that pyrolysis of coal production of synthetic gas system according to embodiments of the present invention takes heat accumulation type radiant tube moving bed
Pyrolysis reactor heats the coal charge of below 20mm, and uniformity of temperature profile, heating effect is good, reaction system simple structure, operation side
Just；Also, pyrolysis gas are not diluted, pyrolysis gas calorific value is high；Pyrolysis reactor is vertical heater simultaneously, and simple structure is saved and built
Cost and floor space；Additionally, set thermal conductor the inner space of the reactor is separated into as the multiple pyrolysis chamber
It is arranged alternately with multiple chambers of multiple radiant tube rooms, and the pyrolysis chamber and radiant tube room, in the case of fully pyrolysis, institute
Stating thermal conductor makes the charging in the heat accumulation type radiant tube of the radiant tube chamber interior and the pyrolysis chamber be separated, utilize
Radiant heat carries out pyrolysis processing to the material in pyrolysis chamber, effectively prevent material and is contacted with heat accumulation type radiant tube, prevents accumulation of heat
The abrasion of formula radiant tube, coking, extend the service life of heat accumulation type radiant tube, improve system operation reliability；And pyrolysis gas
Can be carbon monoxide and hydrogen by methane and a small number of many carbon gaseous hydrocarbons into reburner, synthesize multiple product.
Embodiments in accordance with the present invention, it is adaptable to which the type of furnace of the reactor of the synthesis gas system is not particularly limited,
Can be that thermal storage type moving bed pyrolysis reactor can also be other types, such as non-heat accumulating type or non-moving type, the present invention are excellent
Elect heat accumulation type radiant tube moving bed pyrolysis reactor 3 as, and be vertical heater.
Embodiments in accordance with the present invention, shown in reference picture 1, the pyrolysis reactor 3 includes：Charging aperture 304, pyrolysis gas goes out
Mouth 305, multiple pyrolysis chambers 301 and multiple radiant tube rooms 302, the charging aperture are arranged on the roof of each pyrolysis chamber,
It is described pyrolysis hopper be connected with the charging aperture by first feed arrangement, the pyrolysis gas outlet be arranged on described in each
Be connected on the side wall of radiant tube room and each pyrolysis chamber and with spray column, for pyrolysis gas are passed through in spray column carry out condensation and
Purified treatment, additionally, pyrolysis gas outlet is set on the side wall of each radiant tube room, for spoke will to be entered through the pore area
The a small amount of pyrolysis gas for penetrating pipe chamber interior are discharged by pyrolysis gas outlet, safeguard the environment of radiant tube chamber interior.
Embodiments in accordance with the present invention, shown in reference picture 1, first feed arrangement is connected with the pyrolysis hopper, this
The specific species for inventing first feed arrangement is unrestricted, as long as can effectively convey the pyrolysis material being pyrolyzed in hopper
Into reactor.In some embodiments of the invention, the first feed arrangement 9 can be rotary feeder or helical feed
Machine, the present invention is preferably rotary feeder 9, and thereby, it is possible to realize the Automatic Conveying to pyrolysis material, conveying capacity is controllable, and sets
Standby simple structure, it is easy to operate.
Embodiments in accordance with the present invention, shown in reference picture 1, the thermal conductor 303 laterally has interval along the reactor
Ground is set, and vertically through in the reactor, the inner space of the reactor is separated into as the multiple heat
Multiple chambers of room 301 and multiple radiant tube rooms 302 are solved, and the pyrolysis chamber and radiant tube room are arranged alternately；Wherein, the biography
The specific species of hot body is unrestricted, as long as with the characteristic for readily conducting heat, thermal conductor of the present invention is preferably and readily conducts heat
Metal material, and multiple pore areas are provided with the thermal conductor, the aperture of the pore area is 3-30mm, its total perforate face
Product accounts for the 20-60% of the thermal conductor gross area, enables to heat accumulating type spoke of the material in pyrolysis chamber by radiant tube chamber interior
Pipe is penetrated sufficiently to be pyrolyzed.
Embodiments in accordance with the present invention, shown in reference picture 1, the heat accumulation type radiant tube 306 is provided with：The He of exhanst gas outlet 307
Air intake 308, and the exhanst gas outlet is connected with the drying device, the flue gas discharged by heat accumulation type radiant tube sends into institute
State and material is dried in drying device, by the air intake to being passed through air in the heat accumulation type radiant tube；It is described
Along the short transverse multi-tier arrangement of the reactor in the radiant tube chamber interior, the thermal conductor makes described heat accumulation type radiant tube
Charging in the heat accumulation type radiant tube of radiant tube chamber interior and the pyrolysis chamber is separated, using radiant heat to pyrolysis chamber
Interior material carries out pyrolysis processing, prevents the heat accumulation type radiant tube coking and abrasion；Some embodiments of the invention, this
The concrete shape for inventing the heat accumulation type radiant tube is unrestricted, can be cylindrical or square, and the present invention is preferably
The cylindrical tube of DN200-300, and the level interval of heat accumulation type radiant tube is 200-500mm, vertical interval is 200-700mm,
The heat accumulation type radiant tube number of plies is 10-25 layers, and pyrolysis reactor width is 2-6m, is highly 3-20m.
Embodiments in accordance with the present invention, shown in reference picture 1, spray column of the present invention 10 and the pyrolysis gas outlet 305
Connection, the oil gas discharged by the pyrolysis gas outlet of the radiant tube room and pyrolysis chamber is into being condensed in spray column and purified
Treatment；The tar tank 11 is connected with the spray column 10, it is condensed after cold oil enter the tar tank in store；It is described
Reburner 13 is connected with the spray column, it is purified after not coagulate pyrolysis gas enter reburner, in the reburner, coagulate heat
Vent one's spleen and be converted into synthesis gas；Some embodiments of the invention, the pyrolysis gas that do not coagulate include：Methane and many carbon appropriate hydrocarbon gas,
The synthesis gas is carbon monoxide and Hydrogen synthesis gas, and the fuel cartridge 15 is connected with the reburner 13, and the synthesis gas enters
Enter fuel cartridge to be stored, the multiple products such as methyl alcohol, ethylene glycol, acetic acid can be produced.
Embodiments in accordance with the present invention, shown in reference picture 1, one end and the spray column of combustion gas air-introduced machine of the present invention
Outlet be connected, the other end is connected with the import of the reburner, and the combustion gas is set up between the spray column and reburner
Air-introduced machine, the pyrolysis gas that do not coagulate after quickly and efficiently being purified in spray column are delivered in reburner, are conducive to improving work
Make efficiency.
Embodiments in accordance with the present invention, shown in reference picture 1, second feed arrangement 101 is connected with the loading hopper 1；
The drying device is connected with the exhanst gas outlet on second feed arrangement and the heat accumulation type radiant tube respectively；The gas-solid
Separator is connected with the drying device and the pyrolysis hopper respectively；The exhaust gas cleaner passes through tail gas air-introduced machine
It is connected with the gas-solid separating device；The chimney is connected with the exhaust gas cleaner；Thus, it is possible to pass through the second charging
Device adds the pyrolysis material in loading hopper in drying device, and in drying device, pyrolysis material is from heat accumulation type radiant tube
Flue gas (temperature be 150-250 DEG C) in the presence of be dried, then the mixture of dried pyrolysis material and flue gas enters
Gas-solid separating device, separates the flue gas (temperature be 70-130 DEG C) that obtains into carrying out purified treatment in exhaust gas cleaner, with
Qualified discharge is realized, it is then defeated through the charging aperture by the first feed arrangement that the pyrolysis material that separation is obtained is delivered to pyrolysis hopper
In delivering to the multiple pyrolysis chamber, for carrying out pyrolytic reaction.
Embodiments in accordance with the present invention, shown in reference picture 1, semicoke outlet 309 be arranged on described each pyrolysis chamber and
The bottom of each radiant tube room, the semicoke outlet is connected with semicoke conveying device, and the radiant tube bottom is provided with semicoke outlet,
Discharged for a small amount of pyrolysis material for entering radiant tube chamber interior through the pore area to be exported by semicoke, safeguarded in radiant tube room
The space environment in portion；The semicoke conveying device 14 is preferably conveying worm 14.
Embodiments in accordance with the present invention, the specific species of the second feed device is not particularly limited, as long as be applied to add
Pyrolysis material in hopper is delivered in drying device.In some embodiments of the invention, the second feed device can be
Star feeder or feed screw.Thereby, it is possible to realize the Automatic Conveying to pyrolysis material, and conveying capacity is controllable, equipment knot
Structure is simple, easy to operate.
Embodiments in accordance with the present invention, the specific species of drying device is not particularly limited, as long as can realize to pyrolysis
The drying and preheating of material and the function of lifting.In some embodiments of the invention, drying device 2 is preferably riser and dries
Device 2, thus, pyrolysis material is dried and is lifted in the presence of flue gas, and the mixture of dried pyrolysis material and flue gas is discharged
Riser drier, is conducive to subsequent step to carry out；In drying device, while being dried to pyrolysis material, also realize
The function of preheating, is conducive to improving the speed and efficiency of follow-up pyrolytic reaction, and using the flue gas of heat accumulation type radiant tube discharge
Pyrolysis material is dried and preheated, the comprehensive utilization of heat energy is realized, energy consumption is effectively reduced, the mesh of energy-conserving and environment-protective has been reached
's.
Embodiments in accordance with the present invention, the specific species of gas-solid separating device is not particularly limited, as long as will can be pyrolyzed
Material is separated with flue gas.In some embodiments of the invention, gas-solid separating device 4 can be to dry cyclone separator 4, by
This quickly and efficiently can be separated pyrolysis material and flue gas, and good separating effect, and simple to operate, cost is relatively low.
Embodiments in accordance with the present invention, can also further be set between gas-solid separating device and exhaust gas cleaner 7
There is tail gas air-introduced machine 6, the flue gas that acquisition is separated in gas-solid separating device quickly and efficiently can be delivered to tail by tail gas air-introduced machine
In air purifying apparatus, be conducive to improving operating efficiency.
Embodiments in accordance with the present invention, the system is also provided with the chimney 8 being connected with exhaust gas cleaner, by tail
Flue gas after air purifying apparatus purified treatment is emptied through chimney, thus, is conducive to environmental protection, reduces pollution.
In another aspect of this invention, there is provided a kind of to carry out pyrolysis of coal product conjunction using above-mentioned pyrolysis of coal production of synthetic gas system
Into the method for gas, embodiments in accordance with the present invention comprise the following steps：
A. by granularity for the particulate coal of below 20mm enters riser drier by loading hopper through the second feed arrangement, by heat
The temperature of heat accumulation type radiant tube smoke outlet of reactor is solved for 150-250 DEG C of flue gas is dried and preheats to coal, so
After be lifted into gas-solid separating device, the coal of separation is entered by the first feed arrangement by being pyrolyzed hopper through the charging aperture
It is pyrolyzed in the pyrolysis chamber of the reactor, the flue gas of separation enters exhaust gas cleaner through tail gas air-introduced machine, after purification
Flue gas is discharged through chimney.
Embodiments in accordance with the present invention, shown in reference picture 1, second feed arrangement is connected with the loading hopper；It is described
Drying device is connected with the exhanst gas outlet on second feed arrangement and the heat accumulation type radiant tube respectively；The gas solid separation
Device is connected with the drying device and the pyrolysis hopper respectively；The exhaust gas cleaner passes through tail gas air-introduced machine and institute
Gas-solid separating device is stated to be connected；The chimney is connected with the exhaust gas cleaner.
B. the coal for separate stops 10-100min from top to bottom in described each pyrolysis chamber, divides by with the pyrolysis chamber
High temperature pyrolysis are carried out every the heat accumulation type radiant tube of the radiant tube chamber interior for setting, the high-temperature temperature is 500-600 DEG C, completes heat
Solution preocess, while the temperature for producing is entered for 150-250 DEG C of flue gas by the heat accumulation type radiant tube exhanst gas outlet of pyrolysis reactor
Drying device, recycles.
C. the oil gas of generation is pyrolyzed by the pyrolysis gas outlet of the radiant tube room and pyrolysis chamber into carrying out in spray column
Condensation and purified treatment, are pyrolyzed the semicoke for producing and enter the semicoke through the semicoke outlet of the pyrolysis chamber and radiant tube room bottom
Conveying device is discharged.
Embodiments in accordance with the present invention, shown in reference picture 1, the pyrolysis reactor includes：Charging aperture, pyrolysis gas outlet,
Multiple pyrolysis chambers and multiple radiant tube rooms, the charging aperture are arranged on the roof of each pyrolysis chamber, the pyrolysis hopper
It is connected with the charging aperture by first feed arrangement, the pyrolysis gas outlet is arranged on described each radiant tube room and every
It is connected on the side wall of individual pyrolysis chamber and with spray column, is condensed and purified treatment for pyrolysis gas to be passed through in spray column, this
Outward, pyrolysis gas outlet is set on the side wall of each radiant tube room, for radiant tube chamber interior will to be entered through the pore area
A small amount of pyrolysis gas by pyrolysis gas outlet discharge, safeguard the environment of radiant tube chamber interior.
Embodiments in accordance with the present invention, shown in reference picture 1, semicoke outlet be arranged on described each pyrolysis chamber and each
The bottom of radiant tube room, the semicoke outlet is connected with semicoke conveying device, and the radiant tube bottom is provided with semicoke outlet, is used for
The a small amount of pyrolysis material for entering radiant tube chamber interior through the pore area is exported by semicoke and is discharged, safeguard radiant tube chamber interior
Space environment.
D. the cold oil after condensed enters in tar tank and stores, it is purified after the pyrolysis gas that do not coagulate enter through combustion gas pressure fan
Enter reburner, in the reburner, pyrolysis gas are not coagulated and is converted into synthesis gas.
E. the synthesis gas is stored into fuel cartridge.
Some embodiments of the invention, the pyrolysis gas that do not coagulate include：Methane and many carbon appropriate hydrocarbon gas, the synthesis gas
It is carbon monoxide and Hydrogen synthesis gas, the synthesis gas is stored into fuel cartridge, can produce methyl alcohol, ethylene glycol, acetic acid etc.
Multiple product.
Specific embodiment：Lignite is processed using pyrolysis of coal production of synthetic gas system, the basic data of raw material is shown in Table 1.
Table 1：Lignite basic data
Lignite is processed using the system, pyrolysis gas calorific value is up to 6000kcal/m3, quality is high.System thermal transition efficiency reaches 90%
More than.After heat accumulation type radiant tube was applied through 5000 hours, without coking, wear phenomenon, long service life.
Inventor has found that pyrolysis of coal production of synthetic gas system according to embodiments of the present invention takes heat accumulation type radiant tube moving bed
Pyrolysis reactor heats the coal charge of below 20mm, and uniformity of temperature profile, heating effect is good, reaction system simple structure, operation side
Just；Also, pyrolysis gas are not diluted, pyrolysis gas calorific value is high；Pyrolysis reactor is vertical heater simultaneously, and simple structure is saved and built
Cost and floor space；Additionally, set thermal conductor the inner space of the reactor is separated into as the multiple pyrolysis chamber
It is arranged alternately with multiple chambers of multiple radiant tube rooms, and the pyrolysis chamber and radiant tube room, in the case of fully pyrolysis, institute
Stating thermal conductor makes the charging in the heat accumulation type radiant tube of the radiant tube chamber interior and the pyrolysis chamber be separated, utilize
Radiant heat carries out pyrolysis processing to the material in pyrolysis chamber, effectively prevent material and is contacted with heat accumulation type radiant tube, prevents accumulation of heat
The abrasion of formula radiant tube, coking, extend the service life of heat accumulation type radiant tube, improve system operation reliability；And pyrolysis gas
Can be carbon monoxide and hydrogen by methane and a small number of many carbon gaseous hydrocarbons into reburner, synthesize multiple product.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be fixedly connected, or be detachably connected, or integrally；Can be that machinery connects
Connect, or electrically connect；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, can be in two elements
The connection in portion or two interaction relationships of element.For the ordinary skill in the art, can be according to specific feelings
Condition understands above-mentioned term concrete meaning in the present invention.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be with
It is the first and second feature directly contacts, or the first and second features are by intermediary mediate contact.And, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height less than second feature.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means to combine specific features, structure, material or spy that the embodiment or example are described
Point is contained at least one embodiment of the invention or example.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.And, the specific features of description, structure, material or feature can be any
Combined in an appropriate manner in individual or multiple embodiments or example.Additionally, in the case of not conflicting, the technology of this area
Can be combined for the feature of the different embodiments or example described in this specification and different embodiments or example by personnel
And combination.
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, changes, replacing and modification, simultaneously for those of ordinary skill in the art, according to the think of of the application
Think, will change in specific embodiments and applications.
Claims (10)
1. a kind of pyrolysis of coal production of synthetic gas system, it is characterised in that including：
Pyrolysis hopper；
First feed arrangement, first feed arrangement is connected with the pyrolysis hopper；
Pyrolysis reactor, including：Charging aperture, pyrolysis gas outlet, multiple pyrolysis chambers and multiple radiant tube rooms, the charging aperture are set
On the roof of each pyrolysis chamber, the pyrolysis hopper is connected by first feed arrangement with the charging aperture, institute
Pyrolysis gas outlet is stated to be arranged on the side wall of described each radiant tube room and each pyrolysis chamber, and：
Thermal conductor, the thermal conductor laterally has along the reactor and is positioned apart from, and vertically through in the reactor
It is interior, the inner space of the reactor is separated into the multiple chambers as the multiple pyrolysis chamber and multiple radiant tube rooms, and
The pyrolysis chamber and radiant tube room are arranged alternately；
Heat accumulation type radiant tube, the heat accumulation type radiant tube is along the short transverse multi-tier arrangement of the reactor in the radiant tube room
Inside, the thermal conductor is divided the heat accumulation type radiant tube of the radiant tube chamber interior and the charging in the pyrolysis chamber
Every, using radiant heat pyrolysis processing is carried out to the material in pyrolysis chamber, prevent the heat accumulation type radiant tube coking and abrasion；
Spray column, the spray column is connected with the pyrolysis gas outlet；
Tar tank, the tar tank is connected with the spray column；
Reburner, the reburner is connected with the spray column；
Fuel cartridge, the fuel cartridge is connected with the reburner.
2. system according to claim 1, it is characterised in that multiple pore areas, the pore area are provided with the thermal conductor
Aperture be 3-30mm, its total open area accounts for the 20-60% of the thermal conductor gross area.
3. system according to claim 1, it is characterised in that further include：Combustion gas air-introduced machine, the combustion gas air-introduced machine
One end be connected with the outlet of the spray column, the other end is connected with the import of the reburner.
4. system according to claim 1, it is characterised in that also include：Loading hopper；Second feed arrangement, its with it is described
Loading hopper is connected；Drying device, it connects with the exhanst gas outlet on second feed arrangement and the heat accumulation type radiant tube respectively
Connect；Gas-solid separating device, it is connected with the drying device and the pyrolysis hopper respectively；Exhaust gas cleaner, it passes through
Tail gas air-introduced machine is connected with the gas-solid separating device；Chimney, the chimney is connected with the exhaust gas cleaner.
5. system according to claim 1, it is characterised in that further include that semicoke is exported, the semicoke outlet is set
In described each pyrolysis chamber and the bottom of each radiant tube room, the semicoke outlet is connected with semicoke conveying device.
6. system according to claim 1, it is characterised in that the thermal conductor is readily conduct heat metal material, described first
Feed arrangement is rotary feeder.
7. a kind of method that system using any one of claim 1-5 carries out pyrolysis of coal production of synthetic gas, its feature exists
In comprising the following steps：
A. particulate coal is entered into drying device by loading hopper, by the heat accumulation type radiant tube smoke outlet of pyrolysis reactor
Flue gas is dried and is lifted to coal, and then into gas-solid separating device, the coal of separation is by being pyrolyzed hopper through the charging
Mouthful into being pyrolyzed in the pyrolysis chamber of the reactor, the flue gas of separation enters exhaust gas cleaner through tail gas air-introduced machine, only
Flue gas after change is discharged through chimney；
B. the coal for separate stays for some time from top to bottom in described each pyrolysis chamber, is set by separating with the pyrolysis chamber
The heat accumulation type radiant tube of radiant tube chamber interior carry out high temperature pyrolysis, pyrolytic process is completed, while the flue gas for producing is by pyrolysis
The heat accumulation type radiant tube exhanst gas outlet of reactor enters drying device, recycles；
C. the oil gas of generation is pyrolyzed by the pyrolysis gas outlet of the radiant tube room and pyrolysis chamber into being condensed in spray column
And purified treatment, it is pyrolyzed the semicoke for producing and enters semicoke conveying through the semicoke outlet of the pyrolysis chamber and radiant tube room bottom
Device is discharged；
D. the cold oil after condensed enters in tar tank and stores, it is purified after the pyrolysis gas that do not coagulate enter through combustion gas pressure fan and turn
Change stove, in the reburner, pyrolysis gas are not coagulated and is converted into synthesis gas；
E. the synthesis gas is stored into fuel cartridge.
8. method according to claim 7, it is characterised in that in the step b, the high-temperature temperature is 500-600 DEG C,
The residence time is 10-100min；In the step a and step b, the flue-gas temperature of the radiant tube smoke outlet is
150-250℃。
9. method according to claim 7, it is characterised in that in the step d, the pyrolysis gas that do not coagulate include：Methane
With many carbon appropriate hydrocarbon gas；In the step d and step e, the synthesis gas is carbon monoxide and Hydrogen synthesis gas.
10. method according to claim 7, it is characterised in that the granularity of the particulate coal is below 20mm.
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