CN107723012A - The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling - Google Patents

The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling Download PDF

Info

Publication number
CN107723012A
CN107723012A CN201710831382.6A CN201710831382A CN107723012A CN 107723012 A CN107723012 A CN 107723012A CN 201710831382 A CN201710831382 A CN 201710831382A CN 107723012 A CN107723012 A CN 107723012A
Authority
CN
China
Prior art keywords
coal
gas
pyrolysis
bed
fluidized bed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201710831382.6A
Other languages
Chinese (zh)
Other versions
CN107723012B (en
Inventor
杨占彪
王树宽
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to CN201710831382.6A priority Critical patent/CN107723012B/en
Publication of CN107723012A publication Critical patent/CN107723012A/en
Application granted granted Critical
Publication of CN107723012B publication Critical patent/CN107723012B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • 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
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • 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
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • 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
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Coke Industry (AREA)

Abstract

The present invention relates to the system and method that a kind of multistage fluidized bed pulverized coal pyrolysis and dedusting coupling produce coal tar, coal gas, the system uses gas-solid heat carrier multistage fluidized bed pyrolytic process, raw coke oven gas is pyrolyzed to exchange heat with dried beans after multilevel cyclone dust collection, the purpose that the heavy component of raw coke oven gas is condensed on beans and sweeps along fine powder to reach dedusting with this, simultaneously by the secondary pyrolysis of heavy component, the quality of coal tar is improved；Semicoke after fluidized bed pyrolysis further can include drying unit, fluidized bed pyrolysis and dust removing units, circulation semicoke heating unit, waste heat recovery unit and post-processing unit as the filtrate of granule dedusting after soot blowing to raw coke oven gas dust removal by filtration, system；The quality of the products such as gained coal tar, coal gas and semicoke is high, efficiency of dust collection is high, waste heat recovery, less energy consumption, and small without media regeneration link, whole technique cleaning, energy-conservation, investment.

Description

Multistage fluidized bed pulverized coal pyrolysis and dedusting coupling produce coal-tar gas system and Method
Technical field
The invention belongs to coal chemical industry processing technology field, and in particular to a kind of multistage fluidized bed pulverized coal pyrolysis and dedusting coupling The system for producing coal-tar gas.
Background technology
High-volatile bituminous coal and lignite pyrolysis are the important channels that coal step sub-prime utilizes, and are clean coal chemical technologies, Pyrolysis of coal plant investment is few, and energy consumption is low, and the thermal efficiency is high, and water consumption is few, carbon emission is few, there is extensive market prospects and preferably warp Ji benefit.
Different according to coal particle size, the pyrolytic process of use is also different, and the coal of same particle diameter also has different pyrolytic processes, In numerous pyrolytic processes, fluidized bed pyrolysis mass-and heat-transfer effect is good, but load volume is big, and bigger pressure is brought to follow-up dedusting, Make the high temperature raw coke oven gas for being difficult to dedusting originally be more difficult to tackle, at the same single-stage fluidized bed pyrolysis the residence time it is short, can not to compared with Big particle carries out fully pyrolysis, it is necessary to which coal to be crushed to smaller particle, and the cascade utilization of heat is also not near reasonable.
The macromolecular of high temperature raw coke oven gas coal tar can be condensed carbon distribution, and coal tar will separate out after cooling, generally use now Cyclone dust collectors rough dedusting at high temperature, but do not reach the precision of dedusting, there is the thin dirt in part to enter in condensation in coal tar, Coal tar is caused can not to be subsequently processed further utilizing.Some use subsequent fine dust collecting process, but because regenerative system is too complicated It is difficult to long-term operation.
A kind of fluidized bed coal pyrolysis of Beijing Lei Hao eco-friendly power sources Technology Co., Ltd. Application No. 201520499924.0 System patent, using multicompartment fluidized bed reactor, realize pyrolytic process in fluidized reactor gasification and fluidized-bed reactor Coupling, but just pyrolysis does not reduce fluidized carrier gas to the patented technology using the area of multistage fluidized bed diminution single-stage fluidized bed Amount, and to the UTILIZATION OF VESIDUAL HEAT IN of raw coke oven gas, and rough dedusting is carried out only with cyclone separator in terms of dedusting, for less than 10um Thin dirt can not be removed by cyclone separator, therefore, the dust-laden problem of coal tar is not well solved, coal tar Refined dedusting efficiency is difficult to ensure that.
The content of the invention
In order to overcome the shortcomings of present in the fluidized bed pyrolysis reactor of prior art, the invention provides a kind of multilevel flow Change bed pulverized coal pyrolysis and dedusting coupling produce coal-tar gas system, its be will pyrolysis coupled with dedusting and load volume it is small, flow Change good dedusting effect, the coal tar and gas quality produced are good, and yield is big and plant energy consumption is small.
Meanwhile present invention also offers a kind of method that coal-tar gas is produced with said system, by pyrolysis and dedusting coupling Close, filtrate is without regeneration and heating, and energy consumption is small, and process costs are low.
The technical solution adopted in the present invention is：
The system that coal-tar gas is produced in the multistage fluidized bed pulverized coal pyrolysis and dedusting coupling, including drying unit, fluidisation Bed pyrolysis and dust removing units, circulation semicoke heating unit, waste heat recovery unit and post-processing unit；
Drying unit, using low-heat flue gas caused by waste heat recovery unit as thermal source to fine coal carry out fluidize heat exchange and Heat exchange is connect, it includes multi-stage fluidized bed dryer 1, dedusting combination, and the air guide port of multi-stage fluidized bed dryer 1 combines company with dedusting Logical, dedusting combination is connected with waste heat recovery unit；Being provided with multi-stage fluidized bed dryer 1 can be by hot gas ebullated heat exchange drying The drying chamber 1-2 of fine coal and can be to the heating chamber 1-5 of fine coal indirect heat exchange；
Fluidized bed pyrolysis and dust removing units, dust removal method is pyrolyzed using gas-solid heat carrier multi-stage fluidized, it is pyrolyzed raw coke oven gas Exchanged heat after multilevel cyclone dust collection with dried beans, the heavy component of raw coke oven gas is condensed on beans and swept along carefully with this Powder dedusting, the secondary pyrolysis of heavy component, lighting coal tar；Semicoke after fluidisation pyrolysis can be as granule dedusting after soot blowing Filtrate is further to raw coke oven gas dust removal by filtration；It includes fluidized bed pyrolysis reactor 4 and cross-current type granular-bed filter 12；Institute Stating fluidized bed pyrolysis reactor 4 includes being arranged on reactor shell 4-1 and with the dry coal that multi-stage fluidized bed dryer 1 connects entering Mouth 4g, the raw coke oven gas export mouth 4a connected with the raw coke oven gas entrance of cross-current type granular-bed filter 12, connection is combined with dedusting Dry coal fine powder charging aperture 4b, the semicoke connected with the filtrate entrance of cross-current type granular-bed filter 12 outlet 4e and circulation semicoke The high-temperature semi-coke charging aperture 4c of heating unit connection, the Oil-gas Separation dust outlet 4d and and waste heat connected with post-processing unit The fluidisation gas entry 4f of recovery unit connection, being provided with from top to bottom in reactor shell 4-1 can preheat simultaneously to dry coal Fluidisation heat exchange bed 4-2 to raw coke oven gas filtering, the pyrolysis bed 4-6 that dry coal fluidisation pyrolysis can be made and using fluidizing coal gas double Jiao fluidisation soot blowing soot blowing separation bed 4-9 and can to pyrolysis raw coke oven gas and fluidize coal gas carry out dedusting, Oil-gas Separation it is more Level cyclonic separation combination；Solid overflow is respectively arranged between fluidisation heat exchange bed 4-2 and pyrolysis bed 4-6, soot blowing separation bed 4-9 to lead to Road and gas channel；
Post-processing unit, including oil scrubber 14, the raw coke oven gas outlet of cross-current type granular-bed filter 12 connect with oil scrubber 14 It is logical, make Oil-gas Separation.
Further limit, the fluidized bed pyrolysis reactor 4 includes 2~6 layers of pyrolysis bed 4-6.
Further limit, the multistage cyclone separation combination includes being arranged on fluidisation heat exchange bed 4-2 bottoms and changed with fluidisation The multi-cyclone 4- that the ring baffle 4-3 of air-flow caching chamber is formed between hott bed 4-2 and is arranged on ring baffle 4-3 Extended at the top of 5, multi-cyclone 4-5 above ring baffle 4-3, Oil-gas Separation dust outlet 4d is extended by pipeline To reactor shell 4-1.
Further limit, the solid overflow ducts include connection fluidisation heat exchange bed 4-2 and adjacent pyrolysis bed 4-6 one-level Overflow ducts 4-4, connect the two level overflow ducts 4-8 between soot blowing separation bed 4-9 and adjacent pyrolysis bed 4-6 and connect two-by-two The pyrolysis overflow ducts 4-7 being pyrolyzed between bed 4-6；The dry coal fine powder charging aperture 4b is opened in one-level overflow ducts 4-4 side On wall.
Further limit, height of the feeding mouth higher than corresponding pyrolysis bed 4-6 of the pyrolysis overflow ducts 4-7 upper ends；One Level overflow ducts 4-4 upper end feeding mouth is high higher than fluidisation heat exchange bed 4-2 height, two level overflow ducts 4-8 upper end feeding mouth In orlop pyrolysis bed 4-6 height.
Further limiting, the pyrolysis bed 4-6 and fluidisation heat exchange bed 4-2 and soot blowing separation bed 4-9 are obliquely installed, and with Angle between horizontal plane is for 5 °~25 °.
Further limit, multiple drying beds are provided with from top to bottom in the drying chamber 1-2 of the multi-stage fluidized bed dryer 1 Layer 1-3, air-vent is provided with bed 1-3 is dried, and fine coal overflow pipe 1- is provided between upper and lower dry bed 1-3 4；The heating coil 1-6 with fine coal heat exchange is provided with heating chamber 1-5.
Further limit, the upper port of the fine coal overflow pipe 1-4 dries bed 1-3 higher than corresponding.
Further limit, between the fine coal overflow pipe 1-4 and one-level overflow ducts 4-4, pyrolysis overflow ducts 4- 7th, two level overflow ducts 4-8 is dislocatedly distributed up and down.
Further limit, the circulation semicoke heating unit includes fluidized bed combustor 5, heater riser tube 6, semicoke sedimentation Room 7 and high-temperature flue gas cyclone separator group 8 and afterburning chamber 9；The solid fuel entrance of fluidized bed combustor 5 passes through pipeline point Do not connect with the filtrate outlet of cross-current type granular-bed filter 12 and the Oil-gas Separation dust outlet 4d of fluidized bed pyrolysis reactor 4 It is logical；The outlet of fluidized bed combustor 5 is connected by heater riser tube 6 with the coke powder entrance of semicoke expansion chamber 7；Semicoke expansion chamber 7 High-temperature flue gas outlet connected by pipeline with the smoke inlet of high-temperature flue gas cyclone separator group 8, high-temperature flue gas cyclonic separation The coke powder outlet of device group 8 is extended in semicoke expansion chamber 7, the high-temperature flue gas outlet and afterburning of high-temperature flue gas cyclone separator group 8 Room 9 connects.
Further limit, the waste heat recovery unit includes high-temperature heat-exchanging 10 and desulfuring and denitrifying apparatus 11, the high temperature The high-temperature flue gas entry of heat exchanger 10 connects with afterburning chamber 9, and the low-heat flue gas of high-temperature heat-exchanging 10 passes through desulfuring and denitrifying apparatus 11 Connected with the low-heat smoke inlet of multi-stage fluidized bed dryer 1, circulating gas outlet passes through pipeline and fluidized bed pyrolysis reactor 4 Fluidisation gas entry 4f connection, circulating flue gas outlet mixed with hot air outlet by pipeline after connect with fluidized bed combustor 5 It is logical；
The post-processing unit also includes coke powder cooling waste heat boiler 13, and the semicoke of the coke powder cooling waste heat boiler 13 enters Mouth passes through pipeline and the filtrate outlet of cross-current type granular-bed filter 12 and the Oil-gas Separation dust of fluidized bed pyrolysis reactor 4 Export 4d connections, vapours enters discharge after multi-stage fluidized bed dryer 1 exchanges heat by pipeline and recycled；The oil scrubber 14 Air inlet and cross-current type granular-bed filter 12 raw coke oven gas outlet, oil scrubber gas outlet all the way with high-temperature heat-exchanging 10 circulating gas inlet communications, are connected with coal gas all-product line all the way.
A kind of system that coal-tar gas is produced with above-mentioned multistage fluidized bed pulverized coal pyrolysis and dedusting coupling produces coal tar The method of oil gas, it comprises the following steps：
(1) fine coal is dried
Fluidisation heat exchange removing moisture is carried out to fine coal using 300~380 DEG C of low-heat fume afterheats, recycles steam afterwards Waste heat carries out indirect heat exchange to fine coal and forms dry coal；
(2) fluidisation pyrolysis, dedusting
Fluidisation heat exchange is carried out using high temperature raw coke oven gas and dry coal, dry coal is preheated to 360~380 DEG C, then by waste heat Dry coal mixes further fluidisation pyrolysis with high-temperature semi-coke, produces semicoke；Simultaneously fluidisation coal gas from bottom to top with it is top-down Semicoke adverse current soot blowing, is discharged after making semicoke soot blowing, and fluidize coal gas in flow process with soot blowing fine powder and pyrolysis caused by Raw coke oven gas mixing further makes heavy molecules be cracked into after lighter molecules after multilevel cyclone dust collection is handled and dry coal fluidisation heat exchange Cooling, remaining heavy molecules be attached to after separating out dry coal surface, fine dust also swept along dry coal surface with dry coal from upper and Lower movement, the raw coke oven gas after dedusting further carry out dust removal by filtration by filtrate of the semicoke after soot blowing；Waste coal after dust removal by filtration Gas obtains coal tar and coal gas through Oil-gas Separation, and gained coal tar is as output of products；
(3) semicoke heating is circulated
Solid thermal carriers are produced in semicoke after dust removal by filtration and mixed flue gas mixed combustion, and fluidized bed combustion gas velocity is 0.5~ 5.0m/s, heated to be promoted to 750~850 DEG C, coke powder is used as step (2) after largely being separated by free settling with flue gas dry Pyrolysis of coal thermal source carries out circulating-heating；And afterburning after the further cyclonic separation dedusting of high-temperature flue gas, burn few in high-temperature flue gas The fuel gas and dust of amount；
(4) waste heat recovery
With the high-temperature flue gas of step (3) and air heat exchange occurs for the part coal gas of step (2), reclaims heat, obtains Low-heat flue gas that temperature is 300~380 DEG C, 480~550 DEG C of circulating gas, circulating flue gas that temperature is 450~550 DEG C with And the air that temperature is 450~550 DEG C；Temperature is 300~380 DEG C low-heat flue gas return to step (1) fine coal drying source；Temperature Spend the fluidisation coal gas circulating and recovering for being 480~550 DEG C of circulating gas as step (2)；Temperature is 450~550 DEG C of air With 450~550 DEG C of circulating flue gas return to step (3) of temperature solid thermal carriers are produced as mixed flue gas with coal-char combustion.
Further limit, the step (1) is specifically：
(1.1) fine coal entrance of the 0~6mm fine coal through multi-stage fluidized bed dryer 1 is entered in dryer cartridge 1-1, Flowed from top to bottom through the fine coal overflow pipe 1-4 between multiple dry bed 1-3 in drying chamber 1-2, and with 300~380 DEG C Desulphurization denitration low-heat flue gas carry out fluidisation heat exchange, remove the moisture in fine coal；
(1.2) entered back into after in heating chamber 1-5, with cooling down the row of waste heat boiler 13 from coke powder in heating coil 1-6 The steam that the temperature gone out is 240~300 DEG C carries out indirect heat exchange, and fine coal is preheated；
(1.3) fine coal dried is exported in fluidized bed pyrolysis reactor 4 through dry coal；Flue gas after heat exchange passes through from bottom to top After removing dust combines continuous dust separation again after fine coal coarse filtration, a part exchanges heat again as circulating flue gas through high-temperature heat-exchanging 10 Utilize, part emptying；150~180 DEG C of steam after heat exchange is discharged from heating coil 1-6 steam port, the steaming after discharge The recyclable recycling of vapour.
Further limit, the step (2) is specifically：
(2.1) temperature is that the fluidisation coal gas of 480~550 DEG C of bottom of the circulating gas through fluidized bed pyrolysis reactor 4 enters Mouth 4f enters in reactor shell 4-1 from bottom to top, dry through fluidized bed pyrolysis reactor 4 through step (1) dried dry coal Coal entrance 4g enter reactor shell 4-1 in, fluidisation heat exchange bed 4-2 on the high temperature after multi-cyclone 4-5 dedustings Raw coke oven gas fluidisation heat exchange, makes dry coal be heated to 360~380 DEG C, meanwhile, the heavy molecules in raw coke oven gas are attached to dry after separating out Coal surface, fine dust are also swept along is pyrolyzed chamber on dry coal surface as dry coal enters through one-level overflow ducts 4-4；
(2.2) in chamber is pyrolyzed, the collected dry coal fine powder of dedusting combination enters fluidized bed from dry coal fine powder charging aperture 4b Mixed in pyrolysis reactor 4 with the dry coal after the heating of step (2.1), then the height with 750~850 DEG C of semicoke expansion chamber 7 The mixing of warm semicoke, and further fluidisation pyrolysis, pyrolysis temperature are 480~650 DEG C, and raw coke oven gas caused by pyrolysis is with from reactor Cylinder 4-1 fluidisation coal gas is from bottom to top through multi-cyclone 4-5 dedustings, and the dedusting that cools after fluidizing heat exchange bed 4-2, Discharged afterwards by the raw coke oven gas export mouth 4a at the top of reactor shell 4-1；
(2.3) caused semicoke enters soot blowing separation bed 4-9 with two level overflow ducts 4-8 after being pyrolyzed, from fluidizing coal gas Air-flow drives dust to realize soot blowing to the circulating gas that entrance 4f enters in flow process from bottom to top, and the high-temperature semi-coke after soot blowing is entered Enter filtrate of the cross-current type granular-bed filter 12 as filter；And from the raw coke oven gas export mouth 4a at the top of reactor shell 4-1 Discharge raw coke oven gas passes through 12 further dust removal by filtration of cross-current type granular-bed filter, and the raw coke oven gas after dedusting goes oil scrubber 14 to carry out Oil-gas Separation, the coal gas part after separation return to high-temperature heat-exchanging 10 and carry out heat exchange, a part of conduct as circulating gas Coal gas output of products, and the coal tar isolated exports as tar product.
Further limit, the step (3) is specifically：
The semicoke of cross-current type granular-bed filter 12 after raw coke oven gas dedusting from bottom further to discharging, and and fluid bed heat The Oil-gas Separation mix dust rear portion that solution reactor 4 is discharged go coke powder cooling waste heat boiler 13 cool down after the warehousing that defocuses deposit, A part goes fluidized bed combustor 5 and mixed flue gas mixed combustion to produce solid thermal carriers, and fluidized bed combustion gas velocity is 0.5~ 5.0m/s, then heated riser 6 be further heated to 750~850 DEG C after enter semicoke expansion chamber 7, the gas velocity of heater riser tube 6 15~25m/s, got off into the coke powder in semicoke expansion chamber 7 is most of by free settling, returned through high-temperature semi-coke charging aperture 4c It flow in fluidized bed pyrolysis reactor 4,750~850 containing fine dust DEG C high-temperature flue gas is by high-temperature flue gas whirlwind point simultaneously From afterburning chamber 9 is entered after the dedusting of device group 8, fuel gas and dust a small amount of in high-temperature flue gas, the row of afterburning chamber 9 are further burnt The high-temperature flue gas gone out removes high-temperature heat-exchanging 10；
Further limit, the step (4) is specifically：
From afterburning chamber 9 discharge high-temperature flue gas in high-temperature heat-exchanging 10 with the part after air and step (1) dedusting The part coal gas that flue gas, the oil scrubber 14 of step (2) separate carries out heat exchange, obtains the low-heat cigarette that temperature is 300~380 DEG C Gas, 480~550 DEG C of circulating gas, the circulating flue gas that temperature is 450~550 DEG C and air that temperature is 450~550 DEG C； Temperature is that 300~380 DEG C of low-heat flue gas is done after desulphurization denitration is handled into multistage fluidized bed drier 1 to fine coal It is dry；The circulating gas that temperature is 480~550 DEG C enter from the bottom of fluidized bed pyrolysis reactor 4 and further fluidisation pyrolysis；Temperature Spend 450~550 DEG C of air and the temperature for 450~550 DEG C circulating flue gas mix after be sent into fluidized bed combustor 5 and further fire Burn, make material reuse, waste heat recovery.
The system and method that coal-tar gas is produced in the multistage fluidized bed pulverized coal pyrolysis of the present invention and dedusting coupling is will be more Level pyrolysis bed superposition pyrolysis, to reduce load volume and increase the residence time, while by raw coke oven gas caused by pyrolysis through multi-stage fluidized After bed coarse filtration again through multistage cyclone just dedusting, then with dried cryogenic particles coal carry out heat exchange, make high temperature famine coal The heavy molecules of gas are attached to because cooling separates out can sweep along the fine breeze that raw coke oven gas is carried secretly on dry coal on the surface of coal, both Can with recovery section waste heat again can further dedusting, realize the refined dedusting of raw coke oven gas, greatly improve the efficiency of dust collection of raw coke oven gas, this The outer present invention can also improve the quality of product coal tar, furthermore utilize fluid bed heat by macromolecular tar by being pyrolyzed again Filtrate of the semicoke of reactor discharge as cross-current type granular-bed filter is solved, accomplishes pyrolysis and dedusting coupling, filtrate is without again Raw and heating, the waste heat of raw coke oven gas is taken full advantage of, significantly reduce the energy consumption of device, and gained coal tar, coal gas, half The quality of the products such as coke powder is high, and whole technique simplifies, and Matter Transfer utilizes, heat energy recycle, energy-conservation, reduces investment outlay, and realizes Clean manufacturing.
Brief description of the drawings
Fig. 1 is the process chart that coal-tar gas is produced in the multistage fluidized bed pulverized coal pyrolysis of the present invention and dedusting coupling.
Fig. 2 is the structural representation of multi-stage fluidized bed dryer 1 in Fig. 1.
Fig. 3 is a kind of structural representation of the fluidized bed pyrolysis reactor 4 in Fig. 1.
Fig. 4 is another structural representation of the fluidized bed pyrolysis reactor 4 in Fig. 1.
Fig. 5 is the pyrolysis bed 4-6 structural side views in Fig. 4.
Embodiment
Technical scheme is further described in conjunction with drawings and examples.
As shown in figure 1, the system bag of coal-tar gas is produced in the multistage fluidized bed pulverized coal pyrolysis of the present invention and dedusting coupling Include drying unit, fluidized bed pyrolysis and dust removing units, circulation semicoke heating unit, waste heat recovery unit, post-processing unit；
Drying unit, including multi-stage fluidized bed dryer 1 and dedusting combination, the air guide port of multi-stage fluidized bed dryer 1 with The air inlet connection of dry coal combination cyclone dust collectors 2, dedusting combination combine 3 groups of cyclone dust collectors 2 and sack cleaner by dry coal Into the gas outlet of dry coal combination cyclone dust collectors 2 connects with the air inlet of sack cleaner 3.
As shown in Fig. 2 multi-stage fluidized bed dryer 1 includes dryer cartridge 1-1, opened at the top of dryer cartridge 1-1 Dry coal outlet is offered provided with exhanst gas outlet and fine coal entrance, bottom, fine coal entrance is extended on the outside of dryer cartridge 1-1, is done Coal export is connected by pipeline with the dry coal entrance 4g of fluidized bed pyrolysis reactor 4；Dryer cartridge 1-1 inner chambers are divided into phase up and down Drying chamber 1-2 intercommunicated and that fine coal can be dried by hot gas ebullated heat exchange and can to the heating chamber 1-5 of fine coal indirect heat exchange, 3 dry bed 1-3 or 2~6 are provided with drying chamber 1-2 from top to bottom, dry the minimum between bed 1-3 Spacing is 500mm, can be increased and decreased according to dryer cartridge 1-1 sizes and process lot size, is processed on bed 1-3 is dried Have an air-vent, air-vent can be elongated strip shaped hole or circular port, ventilative to ensure, upper and lower drying bed 1-3 it Between be provided with fine coal overflow pipe 1-4, pass through fine coal overflow pipe 1-4 and realize the fine coal overflow dried up and down between bed 1-3 Circulate, be provided with 2 fine coal overflow pipe 1-4 between 3 dry bed 1-3, fine coal overflow pipe 1-4 corresponding to the superiors Upper port is higher than 80~200mm of upper dry bed 1-3 surfaces, the i.e. a height of 80~200mm in weir, and its lower end is apart from next layer of drying bed Layer 1-3 40~100mm of surface, are embedded in dried coal powder, similarly, fine coal overflow pipe 1-4 upper port is higher than corresponding to intermediate layer Bed 1-3 80~200mm of surface are dried in centre, and its lower end is apart from 40~100mm of lower dry bed 1-3 surfaces.In order to ensure to do Flue gas and fine coal are evenly distributed in dry chamber 1-2 and flue gas can fully contact with fine coal, and upper and lower fine coal overflow pipe 1-4 is carried out It is dislocatedly distributed.Low-heat smoke inlet is provided with below lower dry bed 1-3, low-heat smoke inlet passes through pipeline and waste heat recovery The desulfuring and denitrifying apparatus 11 of unit connects.Heating coil 1-6, heating coil 1-6 steam inlet are provided with heating chamber 1-5 Extended respectively to steam (vapor) outlet outside dryer cartridge 1-1, heating coil 1-6 steam inlet and the coke powder of post-processing unit are cold But the vapours outlet of waste heat boiler 13, heat steam carries out heat exchange with the fine coal in heating chamber 1-5, further by fine coal Heating；150~180 DEG C of steam after heat exchange is discharged from heating coil 1-6 steam port, and the steam after discharge is recyclable sharp again With.
Fluidized bed pyrolysis and dust removing units, including fluidized bed pyrolysis reactor 4 and cross-current type granular-bed filter 12；Institute Stating fluidized bed pyrolysis reactor 4 includes being arranged on reactor shell 4-1 and with the dry coal that multi-stage fluidized bed dryer 1 connects entering Mouth 4g, the raw coke oven gas export mouth 4a connected with the raw coke oven gas entrance of cross-current type granular-bed filter 12, connection is combined with dedusting Dry coal fine powder charging aperture 4b, the semicoke connected with the filtrate entrance of cross-current type granular-bed filter 12 outlet 4e and Oil-gas Separation Dust outlet 4d, high-temperature semi-coke charging aperture 4c and fluidisation gas entry 4f, the raw coke oven gas export at the top of fluidized bed pyrolysis reactor 4 Mouth 4a is connected by pipeline with the air inlet of cross-current type granular-bed filter 12, semicoke outlet 4e passes through pipeline and cross-current type particle The filtrate entrance connection at the top of layer filter 12；The setting number of cross-current type granular-bed filter 12 is reacted according to fluidized bed pyrolysis The semicoke export volume of device 4 determines, can correspond to more cross-current type granular-bed filters of connection in fluidized bed pyrolysis reactor 4 12。
As shown in figure 3, the first implementation situation of fluidized bed pyrolysis reactor 4 is：The fluidized bed pyrolysis reactor 4 includes Reactor shell 4-1, dry coal entrance 4g and raw coke oven gas export mouth 4a are offered at the top of reactor shell 4-1, in reactor Cylinder 4-1 bottom offers fluidisation gas entry 4f, is provided with and dry coal can be preheated simultaneously in reactor shell 4-1 internal upper parts To the fluidisation heat exchange bed 4-2 of raw coke oven gas filtering, bottom, which is provided with, utilizes the soot blowing separation bed for fluidizing double of burnt fluidisation soot blowing of coal gas 4-9, pyrolysis chamber is formed between heat exchange bed 4-2 and soot blowing separation bed 4-9 is fluidized, setting to have three layers in pyrolysis intracavitary can make to do The pyrolysis bed 4-6 of coal fluidisation pyrolysis, pyrolysis bed 4-6 can also be 2~6 layers, but be pyrolyzed bed 4-6 can between 2~6 layers root Adjusted according to reactor shell 4-1 volume size and process lot size.Fluidisation heat exchange bed 4-2 separates with pyrolysis bed 4-6, soot blowing Solid overflow ducts are respectively arranged between bed 4-9, solid is flowed from top to down by solid overflow ducts, solid overflow is led to Road includes connection fluidisation heat exchange bed 4-2 and adjacent pyrolysis bed 4-6 one-level overflow ducts 4-4, connects soot blowing separation bed 4-9 and phase Two level overflow ducts 4-8 and connection between neighbour's pyrolysis bed 4-6 are pyrolyzed the pyrolysis overflow ducts 4-7 between bed 4-6 two-by-two；I.e. The spacing fluidized between the heat exchange bed 4-2 pyrolysis bed 4-6 adjacent with lower section is 3000~5000mm, and is led to by one-level overflow Road 4-4 is connected, and the spacing between soot blowing separation bed 4-9 and adjacent pyrolysis bed 4-6 is 500~600mm, and passes through two level overflow Passage 4-8 is connected, and the spacing between the adjacent pyrolysis bed 4-6 of pyrolysis intracavitary is 500~700mm, and passes through heat between pyrolysis bed 4-6 Solve overflow ducts 4-7 connections.The dry coal fine powder with dry coal fine powder pipeline communication is offered in one-level overflow ducts 4-4 side wall Charging aperture 4b, dry coal fine powder pipeline combine the fine powder buffering chamber connection of cyclone dust collectors 2 with dry coal.Opened in the side wall of pyrolysis chamber Provided with high-temperature semi-coke charging aperture 4c, and high-temperature semi-coke charging aperture 4c, dry coal fine powder charging aperture 4b are arranged on the pyrolysis bed of the superiors Above 4-6, sunk by the high-temperature semi-coke passage on high-temperature semi-coke charging aperture 4c with circulating the semicoke of semicoke heating unit The semicoke outlet of room 7 drops.Corresponding to soot blowing separation bed 4-9 two are being offered on reactor shell 4-1 side walls or bottom Semicoke discharging opening 4e, connected by semicoke entrances of the semicoke discharging opening 4e respectively with two cross-current type granular-bed filters 12.Half Burnt discharging opening 4e in soot blowing separation bed 4-9 top, can be opened up along in reactor shell 4-1 side walls it is multiple, and It is evenly distributed on reactor shell 4-1, the semicoke product after soot blowing is drained into by cross-current type stratum granulosum by semicoke discharging opening 4e Filter 12.Multistage cyclone separation combination is provided with fluidisation heat exchange bed 4-2 bottom, multistage cyclone separation combination includes annular Baffle plate 4-3 and multi-cyclone 4-5, ring baffle 4-3 are concave plates, are arranged on fluidisation heat exchange bed 4-2 bottom, make ring Air-flow caching chamber is formed between shape baffle plate 4-3 and fluidisation heat exchange bed 4-2, circular hole is offered at ring baffle 4-3 center simultaneously Multi-cyclone 4-5 is installed thereon, the multi-cyclone 4-5 of the present embodiment includes one cyclonic and two level Whirlwind cyclone, one cyclonic and the series connection of two level Whirlwind cyclone, i.e. the purification gas outlet of one cyclonic and the air inlet of two level Whirlwind cyclone Mouth connection, the purification gas outlet of two level Whirlwind cyclone extend to ring baffle 4-3 centre bore, one cyclonic and two level Whirlwind cyclone Feed opening be that Oil-gas Separation dust outlet 4d is extended on the outside of reactor shell 4-1.In order to ensure the weight in high temperature raw coke oven gas Lighter molecules are formed after the pyrolysis of matter molecule, and the raw coke oven gas being pyrolyzed can be carried out with the fluidisation heat exchange bed 4-2 on upper strata fine coal Heat exchange, multi-cyclone 4-5 is arranged on above pyrolysis intracavitary the superiors pyrolysis bed 4-6, produced through being pyrolyzed chamber pyrolysis Raw coke oven gas and fluidisation raw coke oven gas be mixed into multi-cyclone 4-5 through one-level, two level Whirlwind cyclone carry out one-level remove Dirt and two-stage dust removal, through fluidizing heat exchange bed 4-2 with fine coal heat exchange occurs for raw coke oven gas after dedusting, is heated fine coal, raw coke oven gas Discharged after cooling down through raw coke oven gas export mouth 4a.Multi-cyclone 4-5 whirlwind subseries can also be according to dedusting Amount size is adjusted.
In order to ensure that reactor shell 4-1 interior air-flows are smooth, in pyrolysis bed 4-6 and fluidisation heat exchange bed 4-2, soot blowing separation bed Bar shaped airflow hole is offered on 4-9, forms gas channel；The percent opening of bar shaped airflow hole is 5%~25%.Bar shaped airflow hole Tilted in pyrolysis bed 4-6, fluidisation heat exchange bed 4-2, soot blowing separation bed 4-9 thickness direction, inclination angle is 5 °~25 °, in order to solid The flowing of body material.
In order to ensure that gas and fine coal have certain time of contact, and fine coal is evenly distributed under airflow function, and above-mentioned one Level overflow ducts 4-4 upper end feeding mouth be higher by fluidisation heat exchange bed 4-2 80~200mm of surface and lower end apart from the superiors pyrolysis Bed 4-6 40~100mm of surface；The upper end feeding mouth of the two level overflow ducts 4-8 be higher by orlop pyrolysis bed 4-6 surfaces 80~ The upper end feeding mouth of 200mm and lower end apart from soot blowing separation bed 4-9 40~100mm of surface, thermal decomposition tube 4-7 roads is higher by corresponding pyrolysis Bed 4-6 80~200mm of surface and lower end is apart from lower floor pyrolysis bed 4-6 40~100mm of surface.In addition, the one-level of the present embodiment is overflow Circulation road 4-4, pyrolysis overflow ducts 4-7, two level overflow ducts 4-8 are dislocatedly distributed up and down.
As shown in figure 4, second of implementation situation of the fluidized bed pyrolysis reactor 4 of the present embodiment is：The fluidized bed pyrolysis Reactor 4 includes reactor shell 4-1, and dry coal entrance 4g and raw coke oven gas export mouth are offered at the top of reactor shell 4-1 4a, fluidisation gas entry 4f is offered in reactor shell 4-1 bottom, reactor shell 4-1 internal upper parts are provided with fluidisation Heat exchange bed 4-2, bottom are provided with soot blowing separation bed 4-9, and pyrolysis is formed between heat exchange bed 4-2 and soot blowing separation bed 4-9 is fluidized Chamber, pyrolysis intracavitary is provided with 2 layers of pyrolysis bed 4-6, can be between 2~6 layers according to reactor shell 4- but be pyrolyzed bed 4-6 1 volume size and process lot size adjustment.Led between fluidisation heat exchange bed 4-2 and adjacent pyrolysis bed 4-6 by one-level overflow Road 4-4 is connected, and is connected between soot blowing separation bed 4-9 and adjacent pyrolysis bed 4-6 by two level overflow ducts 4-8, one layer of pyrolysis bed Connected by being pyrolyzed overflow ducts 4-7 between 4-6 and adjacent one layer pyrolysis bed 4-6, opened in one-level overflow ducts 4-4 side wall Provided with the dry coal fine powder charging aperture 4b with dry coal fine powder pipeline communication, dry coal fine powder pipeline combines cyclone dust collectors 2 with dry coal Fine powder buffering chamber connects.High-temperature semi-coke charging aperture 4c is being offered in reactor shell 4-1 side walls corresponding to pyrolysis bed 4-6, is being led to The semicoke outlet of the high-temperature semi-coke passage crossed on high-temperature semi-coke charging aperture 4c and semicoke expansion chamber 7, in soot blowing point From semicoke discharging opening 4e is offered corresponding to bed 4-9 on reactor shell 4-1 bottoms, pass through semicoke discharging opening 4e and cross-current type The semicoke entrance connection of granulosa filter 12.
The pyrolysis bed 4-6 and fluidisation heat exchange bed 4-2 and soot blowing separation bed 4-9 of the present embodiment are obliquely installed, and fluidisation is changed Inclination side between hott bed 4-2 and adjacent pyrolysis bed 4-6, soot blowing separation bed 4-9 and adjacent soot blowing separation bed 4-9, pyrolysis bed 4-6 To on the contrary, angle of inclination be 5 °~25 ° in the range of it is adjustable, be easy to fine coal under air-flow impetus to underflow stream.In order to ensure The time of contact of raw coke oven gas and semicoke, the minimum fluidized between the heat exchange bed 4-2 pyrolysis bed 4-6 adjacent with lower section of the present embodiment Spacing is 3000mm, and the minimum spacing between soot blowing separation bed 4-9 and adjacent pyrolysis bed 4-6 is 600mm, antipyretic intracavitary adjacent heat It is 500 to solve the minimum spacing between bed 4-6.The one-level overflow ducts 4-4, pyrolysis overflow ducts 4-7 and two level of the present embodiment Overflow ducts 4-8 is dislocatedly distributed up and down along reactor shell 4-1, and it is equal to ensure that fine coal, semicoke can be distributed on corresponding bed It is even.
The present embodiment is provided with multistage cyclone separation combination, multistage cyclone separation combination in fluidisation heat exchange bed 4-2 bottom Including ring baffle 4-3 and multi-cyclone 4-5, ring baffle 4-3 is concave plate, is arranged on fluidisation heat exchange bed 4-2's Bottom, make to form air-flow caching chamber between ring baffle 4-3 and fluidisation heat exchange bed 4-2, opened up at ring baffle 4-3 center There is circular hole and multi-cyclone 4-5 is installed thereon, the multi-cyclone 4-5 of the present embodiment includes one cyclonic Son and two level Whirlwind cyclone, one cyclonic and the series connection of two level Whirlwind cyclone, i.e. the purification gas outlet of one cyclonic and two level whirlwind The air inlet connection of son, the purification gas outlet of two level Whirlwind cyclone are extended on the upside of ring baffle 4-3, one cyclonic and two level rotation The feed opening of wind is extended on the outside of reactor shell 4-1.
In order to ensure that reactor shell 4-1 interior air-flows are smooth, in pyrolysis bed 4-6 and fluidisation heat exchange bed 4-2, soot blowing separation bed Bar shaped airflow hole is offered on 4-9, forms gas channel；The percent opening of bar shaped airflow hole is 5%~25%.Bar shaped airflow hole Tilted in pyrolysis bed 4-6, fluidisation heat exchange bed 4-2, soot blowing separation bed 4-9 thickness direction, inclination angle is 5 °~25 °, in order to solid The flowing of body material, as shown in Figure 5.
Circulate semicoke heating unit, including fluidized bed combustor 5, heater riser tube 6, semicoke expansion chamber 7 and high temperature cigarette Cyclonic wind separator group 8；The solid fuel entrance of fluidized bed combustor 5 passes through Y tube and cross-current type granular-bed filter 12 Filtrate exports and the Oil-gas Separation dust outlet 4d of fluidized bed pyrolysis reactor 4 connections, the high-temperature gas of fluidized bed combustor 5 Entrance connects with high-temperature heat-exchanging 10；The coke powder that the outlet of fluidized bed combustor 5 passes through heater riser tube 6 and semicoke expansion chamber 7 Entrance connects；The high-temperature flue gas outlet of semicoke expansion chamber 7 is connected by pipeline and the smoke inlet of high-temperature flue gas cyclone separator group 8 Logical, the exhanst gas outlet of high-temperature flue gas cyclone separator group 8 is connected by pipeline with afterburning chamber 9, few in flammable burn-up high-temperature flue gas The fuel gas and dust of amount, the coke powder outlet of high-temperature flue gas cyclone separator group 8 are extended in semicoke expansion chamber 7；
Waste heat recovery unit, including high-temperature heat-exchanging 10 and desulfuring and denitrifying apparatus 11, the high temperature of the high-temperature heat-exchanging 10 Smoke inlet is connected by pipeline with the exhanst gas outlet of afterburning chamber 9, exhanst gas outlet and the high-temperature heat-exchanging 10 of sack cleaner 3 Circulating flue gas entrance connects, and the low-heat flue gas of high-temperature heat-exchanging 10 passes through desulfuring and denitrifying apparatus 11 and multi-stage fluidized bed dryer 1 The connection of low-heat smoke inlet, circulating gas outlet connected by the fluidisation gas entry 4f of pipeline and fluidized bed pyrolysis reactor 4 Logical, hot air outlet is exported by being connected after pipeline mixing with fluidized bed combustor 5 with circulating flue gas；
Post-processing unit, including coke powder cooling waste heat boiler 13 and oil scrubber 14, the coke powder cooling waste heat boiler 13 Semicoke entrance passes through the outlet of the filtrate of pipeline and cross-current type granular-bed filter 12 and the oil gas point of fluidized bed pyrolysis reactor 4 Entered from dust outlet 4d connections, vapours by pipeline after multi-stage fluidized bed dryer 1 exchanges heat and discharged；The oil scrubber 14 The raw coke oven gas outlet of air inlet and cross-current type granular-bed filter 12, the gas outlet of oil scrubber 14 is returned all the way by pipeline Return high-temperature heat-exchanging 10 and carry out heat exchange as circulating gas, a part is used as coal gas output of products.
The system that coal-tar gas is produced with above-mentioned multistage fluidized bed pulverized coal pyrolysis and dedusting coupling produces coal-tar gas Method realized by following steps：
(1) fine coal is dried
Fluidisation heat exchange removing moisture is carried out to fine coal using 300~380 DEG C of low-heat fume afterheats, recycles steam afterwards Waste heat carries out indirect heat exchange to fine coal and forms dry coal；Specifically include following steps：
(1.1) fine coal entrance of the 0~6mm fine coal through multi-stage fluidized bed dryer 1 is entered in dryer cartridge 1-1, Flowed from top to bottom through the fine coal overflow pipe 1-4 between multiple dry bed 1-3 in drying chamber 1-2, and with 300~380 DEG C Desulphurization denitration low-heat flue gas carry out fluidisation heat exchange, remove the moisture in fine coal；
(1.2) entered back into after in heating chamber 1-5, with cooling down the row of waste heat boiler 13 from coke powder in heating coil 1-6 The steam that the temperature gone out is 240~300 DEG C carries out indirect heat exchange, and fine coal is preheated；
(1.3) fine coal dried is exported in fluidized bed pyrolysis reactor 4 through dry coal；Flue gas after heat exchange passes through from bottom to top After removing dust combines continuous dust separation again after fine coal coarse filtration, a part exchanges heat again as circulating flue gas through high-temperature heat-exchanging 10 Utilize, part emptying；150~180 DEG C of steam after heat exchange is discharged from heating coil 1-6 steam port, the steaming after discharge The recyclable recycling of vapour.
(2) fluidisation pyrolysis, dedusting
Fluidisation heat exchange is carried out using high temperature raw coke oven gas and dry coal, dry coal is preheated to 360~380 DEG C, then by waste heat Dry coal mixes further fluidisation pyrolysis with high-temperature semi-coke, produces semicoke；Simultaneously fluidisation coal gas from bottom to top with it is top-down Semicoke adverse current soot blowing, is discharged after making semicoke soot blowing, and fluidize coal gas in flow process with soot blowing fine powder and pyrolysis caused by It is cold that raw coke oven gas mixing further makes heavy molecules be cracked into after lighter molecules the dry coal fluidisation heat exchange after multilevel cyclone dust collection is handled But, remaining heavy molecules be attached to after separating out dry coal surface, fine dust also swept along dry coal surface with dry coal from top to bottom Mobile, the raw coke oven gas after dedusting further carries out dust removal by filtration by filtrate of the semicoke after soot blowing；Raw coke oven gas after dust removal by filtration Coal tar and coal gas are obtained through Oil-gas Separation, gained coal tar is as output of products；Specifically realized by following steps：
(2.1) temperature is that the fluidisation coal gas of 480~550 DEG C of bottom of the circulating gas through fluidized bed pyrolysis reactor 4 enters Mouth 4f enters in reactor shell 4-1 from bottom to top, dry through fluidized bed pyrolysis reactor 4 through step (1) dried dry coal Coal entrance 4g enter reactor shell 4-1 in, fluidisation heat exchange bed 4-2 on the high temperature after multi-cyclone 4-5 dedustings Raw coke oven gas fluidisation heat exchange, makes dry coal be heated to 360~380 DEG C, meanwhile, the heavy molecules in raw coke oven gas are attached to dry after separating out Coal surface, fine dust are also swept along is pyrolyzed chamber on dry coal surface as dry coal enters through one-level overflow ducts 4-4；
(2.2) in chamber is pyrolyzed, the collected dry coal fine powder of dedusting combination enters fluidized bed from dry coal fine powder charging aperture 4b Mixed in pyrolysis reactor 4 with the dry coal after the heating of step (2.1), then the height with 750~850 DEG C of semicoke expansion chamber 7 The mixing of warm semicoke, and further fluidisation pyrolysis, pyrolysis temperature are 480~650 DEG C, and raw coke oven gas caused by pyrolysis is with from reactor Cylinder 4-1 fluidisation coal gas is from bottom to top through multi-cyclone 4-5 dedustings, and the dedusting that cools after fluidizing heat exchange bed 4-2, Discharged afterwards by the raw coke oven gas export mouth 4a at the top of reactor shell 4-1；
(2.3) caused semicoke enters soot blowing separation bed 4-9 with two level overflow ducts 4-8 after being pyrolyzed, from fluidizing coal gas Air-flow drives dust to realize soot blowing to the circulating gas that entrance 4f enters in flow process from bottom to top, and the high-temperature semi-coke after soot blowing is entered Enter filtrate of the cross-current type granular-bed filter 12 as filter；And from the raw coke oven gas export mouth 4a at the top of reactor shell 4-1 Discharge raw coke oven gas passes through 12 further dust removal by filtration of cross-current type granular-bed filter, and the raw coke oven gas after dedusting goes oil scrubber 14 to carry out Oil-gas Separation, the coal gas part after separation return to high-temperature heat-exchanging 10 and carry out heat exchange, a part of conduct as circulating gas Coal gas output of products, and the coal tar isolated is as output of products.
(3) semicoke heating is circulated
Solid thermal carriers are produced in semicoke after dust removal by filtration and mixed flue gas mixed combustion, and fluidized bed combustion gas velocity is 0.5~ 5.0m/s, heated to be promoted to 750~850 DEG C, coke powder is used as step (2) after largely being separated by free settling with flue gas dry Pyrolysis of coal thermal source carries out circulating-heating；And afterburning after the further cyclonic separation dedusting of high-temperature flue gas, burn few in high-temperature flue gas The fuel gas and dust of amount；
Specifically：The semicoke of cross-current type granular-bed filter 12 further to after raw coke oven gas dedusting from bottom discharge, and with The Oil-gas Separation mix dust rear portion that fluidized bed pyrolysis reactor 4 is discharged goes coke powder cooling waste heat boiler 13 to be defocused after cooling down Warehousing is deposited, and a part goes fluidized bed combustor 5 to produce solid thermal carriers with mixed flue gas mixed combustion, and fluidized bed combustion gas velocity is 0.5~5.0m/s, then heated riser 6 be further heated to 750~850 DEG C after enter semicoke expansion chamber 7, heater riser tube 6 15~25m/s of gas velocity, got off into the coke powder in semicoke expansion chamber 7 is most of by free settling, through high-temperature semi-coke charging aperture 4c is back in fluidized bed pyrolysis reactor 4, and 750~850 containing fine dust DEG C high-temperature flue gas revolves by high-temperature flue gas simultaneously Enter afterburning chamber 9 after the dedusting of wind separator group 8, further burn fuel gas and dust a small amount of in high-temperature flue gas, afterburning The high-temperature flue gas that room 9 is discharged removes high-temperature heat-exchanging 10；
(4) waste heat recovery
From afterburning chamber 9 discharge high-temperature flue gas in high-temperature heat-exchanging 10 with the part after air and step (1) dedusting The part coal gas that flue gas, the oil scrubber 14 of step (2) separate carries out heat exchange, obtains the low-heat cigarette that temperature is 300~380 DEG C Gas, 480~550 DEG C of circulating gas, the circulating flue gas that temperature is 450~550 DEG C and air that temperature is 450~550 DEG C； Temperature is that 300~380 DEG C of low-heat flue gas is done after desulphurization denitration is handled into multistage fluidized bed drier 1 to fine coal It is dry；The circulating gas that temperature is 480~550 DEG C enter from the bottom of fluidized bed pyrolysis reactor 4 and further fluidisation pyrolysis；Temperature Spend 450~550 DEG C of air and the temperature for 450~550 DEG C circulating flue gas mix after be sent into fluidized bed combustor 5 and further fire Burn, make material reuse, waste heat recovery.
Involved process conditions can adjust in corresponding effective scope in the above method, not detailed in above-described embodiment The structure of explanation and the part of annexation belong to the conversion of the ordinary skill in the art, for the contents of the section, this Art personnel can realize according to conventional technical means.

Claims (16)

1. the system that coal-tar gas is produced in a kind of multistage fluidized bed pulverized coal pyrolysis and dedusting coupling, it is characterised in that system includes Drying unit, fluidized bed pyrolysis and dust removing units, circulation semicoke heating unit, waste heat recovery unit and post-processing unit；
Drying unit, fluidisation heat exchange is carried out to fine coal as thermal source using low-heat flue gas caused by waste heat recovery unit and is changed indirectly Heat, it includes multi-stage fluidized bed dryer (1), dedusting combination, and the air guide port of multi-stage fluidized bed dryer (1) combines company with dedusting Logical, dedusting combination is connected with waste heat recovery unit；Being provided with multi-stage fluidized bed dryer (1) can be dry by hot gas ebullated heat exchange The drying chamber (1-2) of dry fine coal and can be to the heating chamber (1-5) of fine coal indirect heat exchange；
Fluidized bed pyrolysis and dust removing units, dust removal method is pyrolyzed using gas-solid heat carrier multi-stage fluidized, it is more that it is pyrolyzed raw coke oven gas warp Exchanged heat after level cyclone dust removal with dried beans, the heavy component of raw coke oven gas is condensed on beans and sweeps along fine powder to remove with this Dirt, the secondary pyrolysis of heavy component, lighting coal tar；Semicoke after fluidisation pyrolysis can be as the filtrate of granule dedusting after soot blowing Further to raw coke oven gas dust removal by filtration；It includes fluidized bed pyrolysis reactor (4) and cross-current type granular-bed filter (12)；Institute Stating fluidized bed pyrolysis reactor (4) includes what is be arranged on reactor shell (4-1) and connected with multi-stage fluidized bed dryer (1) Dry coal entrance (4g), the raw coke oven gas export mouth (4a) connected with the raw coke oven gas entrance of cross-current type granular-bed filter (12), with removing The dry coal fine powder charging aperture (4b) of dirt combination connection, the semicoke connected with the filtrate entrance of cross-current type granular-bed filter (12) go out Mouthful (4e), with circulating the semicoke heating unit high-temperature semi-coke charging aperture (4c) connected, the Oil-gas Separation connected with post-processing unit Dust outlet (4d) and the fluidisation gas entry (4f) connected with waste heat recovery unit, from upper in reactor shell (4-1) And it is arranged with the fluidisation heat exchange bed (4-2) that can be preheated to dry coal and be filtered to raw coke oven gas, dry coal fluidisation pyrolysis can be made Pyrolysis bed (4-6) and using fluidizing the coal gas half-and-half soot blowing separation bed (4-9) of burnt fluidisation soot blowing and can be to being pyrolyzed waste coal Gas carries out dedusting with fluidisation coal gas, the multistage cyclone of Oil-gas Separation separates combination；Fluidize heat exchange bed (4-2) with pyrolysis bed (4-6), Solid overflow ducts and gas channel are respectively arranged between soot blowing separation bed (4-9)；
Post-processing unit, including oil scrubber (14), raw coke oven gas outlet and the oil scrubber (14) of cross-current type granular-bed filter (12) Connection, makes Oil-gas Separation.
2. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 1 and dedusting coupling, its It is characterised by：The fluidized bed pyrolysis reactor (4) includes 2~6 layers of pyrolysis bed (4-6).
3. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 1 and dedusting coupling, its It is characterised by：The multistage cyclone separation combination includes being arranged on fluidisation heat exchange bed (4-2) bottom and with fluidizing heat exchange bed (4-2) Between form the ring baffle (4-3) of air-flow caching chamber and the multi-cyclone (4- that is arranged on ring baffle (4-3) 5), extended at the top of multi-cyclone (4-5) above ring baffle (4-3), Oil-gas Separation dust outlet (4d) passes through It is outside that pipeline extends to reactor shell (4-1).
4. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 1 and dedusting coupling, its It is characterised by：The solid overflow ducts include connection fluidisation heat exchange bed (4-2) and the one-level overflow of adjacent pyrolysis bed (4-6) is led to Road (4-4), connection soot blowing separation bed (4-9) and the adjacent two level overflow ducts (4-8) being pyrolyzed between bed (4-6) and connect two Pyrolysis overflow ducts (4-7) between two pyrolysis beds (4-6)；The dry coal fine powder charging aperture (4b) is opened in one-level overflow ducts In the side wall of (4-4).
5. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 4 and dedusting coupling, its It is characterised by：Height of the feeding mouth of described pyrolysis overflow ducts (4-7) upper end higher than corresponding pyrolysis bed (4-6)；One-level overflow The upper end feeding mouth of passage (4-4) is high higher than fluidisation heat exchange bed (4-2) height, the upper end feeding mouth of two level overflow ducts (4-8) In the height of orlop pyrolysis bed (4-6).
6. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 4 and dedusting coupling, its It is characterised by：It is described pyrolysis bed (4-6) and fluidize heat exchange bed (4-2) and soot blowing separation bed (4-9) be obliquely installed, and with level Angle between face is for 5 °~25 °.
7. the multistage fluidized bed pulverized coal pyrolysis and dedusting coupling according to any one of claim 1~6 produce coal-tar gas System, it is characterised in that：It is provided with from top to bottom in the drying chamber (1-2) of the multi-stage fluidized bed dryer (1) multiple dry Dry bed (1-3), air-vent is provided with bed (1-3) is dried, and fine coal is provided between upper and lower dry bed (1-3) Overflow pipe (1-4)；The heating coil (1-6) with fine coal heat exchange is provided with heating chamber (1-5).
8. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 7 and dedusting coupling, its It is characterised by：The upper port of the fine coal overflow pipe (1-4) dries bed (1-3) higher than corresponding.
9. multistage fluidized bed reactor according to claim 8, multi-stage fluidized bed dryer, it is characterised in that：The powder Between coal overflow pipe (1-4) and one-level overflow ducts (4-4), pyrolysis overflow ducts (4-7), two level overflow ducts (4-8) It is dislocatedly distributed up and down.
10. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 9 and dedusting coupling, its It is characterised by：The circulation semicoke heating unit includes fluidized bed combustor (5), heater riser tube (6), semicoke expansion chamber (7) And high-temperature flue gas cyclone separator group (8) and afterburning chamber (9)；The solid fuel entrance of fluidized bed combustor (5) passes through pipe Road is exported respectively with the filtrate of cross-current type granular-bed filter (12) and the Oil-gas Separation dust of fluidized bed pyrolysis reactor (4) Export (4d) connection；The outlet of fluidized bed combustor (5) passes through heater riser tube (6) and the coke powder entrance of semicoke expansion chamber (7) Connection；The high-temperature flue gas outlet of semicoke expansion chamber (7) is connected by pipeline and the smoke inlet of high-temperature flue gas cyclone separator group (8) Logical, the coke powder outlet of high-temperature flue gas cyclone separator group (8) is extended in semicoke expansion chamber (7), high-temperature flue gas cyclone separator The high-temperature flue gas outlet of group (8) connects with afterburning chamber (9).
11. the system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis according to claim 10 and dedusting coupling, It is characterized in that：The waste heat recovery unit includes high-temperature heat-exchanging (10) and desulfuring and denitrifying apparatus (11), the high temperature heat exchange The high-temperature flue gas entry of device (10) connects with afterburning chamber (9), and the low-heat flue gas of high-temperature heat-exchanging (10) passes through desulfuring and denitrifying apparatus (11) connected with the low-heat smoke inlet of multi-stage fluidized bed dryer (1), circulating gas outlet passes through pipeline and fluidized bed pyrolysis Reactor (4) fluidisation gas entry (4f) connection, circulating flue gas outlet mixed with hot air outlet by pipeline after with fluidisation Bed burner (5) connection；
The post-processing unit also includes coke powder cooling waste heat boiler (13), and the semicoke of the coke powder cooling waste heat boiler (13) enters Mouth passes through pipeline and the filtrate outlet of cross-current type granular-bed filter (12) and the Oil-gas Separation of fluidized bed pyrolysis reactor (4) Dust outlet (4d) connection, vapours enter after multi-stage fluidized bed dryer (1) heat exchange to discharge by pipeline to be recycled；It is described The air inlet of oil scrubber (14) and the raw coke oven gas outlet of cross-current type granular-bed filter (12), oil scrubber gas outlet is all the way With high-temperature heat-exchanging (10) circulating gas inlet communication, connected all the way with coal gas all-product line.
A kind of 12. system that coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling with described in claim 1 The method for producing coal-tar gas, it is characterised in that comprise the following steps：
(1) fine coal is dried
Fluidisation heat exchange removing moisture is carried out to fine coal using 300~380 DEG C of low-heat fume afterheats, recycles steam waste heat afterwards Indirect heat exchange is carried out to fine coal and forms dry coal；
(2) fluidisation pyrolysis, dedusting
Fluidisation heat exchange is carried out using high temperature raw coke oven gas and dry coal, dry coal is preheated to 360~380 DEG C, then the dry coal by waste heat Further fluidisation pyrolysis is mixed with high-temperature semi-coke, produces semicoke；Fluidisation coal gas from bottom to top and top-down semicoke simultaneously Adverse current soot blowing, discharged after making semicoke soot blowing, and fluidize coal gas in flow process with soot blowing fine powder and pyrolysis caused by waste coal Gas mixing further make heavy molecules be cracked into after lighter molecules after multilevel cyclone dust collection is handled with dry coal fluidize heat exchange cooling, Remaining heavy molecules are attached to dry coal surface, fine dust after separating out and also swept along on dry coal surface as dry coal moves from top to bottom Dynamic, the raw coke oven gas after dedusting further carries out dust removal by filtration by filtrate of the semicoke after soot blowing；Raw coke oven gas warp after dust removal by filtration Oil-gas Separation obtains coal tar and coal gas, and gained coal tar is as output of products；
(3) semicoke heating is circulated
Semicoke after dust removal by filtration produces solid thermal carriers with mixed flue gas mixed combustion, and fluidized bed combustion gas velocity is 0.5~5.0m/ S, heated to be promoted to 750~850 DEG C, coke powder is used as step (2) dry coal heat after largely being separated by free settling with flue gas Solve thermal source and carry out circulating-heating；And afterburning after the further cyclonic separation dedusting of high-temperature flue gas, burn in high-temperature flue gas a small amount of Fuel gas and dust；
(4) waste heat recovery
With the high-temperature flue gas of step (3) and air heat exchange occurs for the part coal gas of step (2), reclaims heat, obtains temperature For 300~380 DEG C of low-heat flue gas, 480~550 DEG C of circulating gas, the circulating flue gas that temperature is 450~550 DEG C and temperature Spend the air for 450~550 DEG C；Temperature is 300~380 DEG C low-heat flue gas return to step (1) fine coal drying source；Temperature is Fluidisation coal gas circulating and recovering of 480~550 DEG C of the circulating gas as step (2)；The air that temperature is 450~550 DEG C and temperature The circulating flue gas return to step (3) of 450~550 DEG C of degree produces solid thermal carriers as mixed flue gas with coal-char combustion.
13. the method according to claim 12 for producing coal-tar gas, it is characterised in that the step (1) is specifically：
(1.1) fine coal entrance of the 0~6mm fine coal through multi-stage fluidized bed dryer (1) is entered in dryer cartridge (1-1), Flowed from top to bottom through the fine coal overflow pipe (1-4) between multiple dry beds (1-3) in drying chamber (1-2), and with 300~ 380 DEG C of desulphurization denitration low-heat flue gas carries out fluidisation heat exchange, removes the moisture in fine coal；
(1.2) entered back into after in heating chamber (1-5), with cooling down waste heat boiler (13) from coke powder in heating coil (1-6) The steam that the temperature of discharge is 240~300 DEG C carries out indirect heat exchange, and fine coal is preheated；
(1.3) fine coal dried is exported in fluidized bed pyrolysis reactor (4) through dry coal；Flue gas after heat exchange is from bottom to top through powder After removing dust combines continuous dust separation again after coal coarse filtration, a part exchanges heat again as circulating flue gas through high-temperature heat-exchanging (10) Utilize, part emptying；150~180 DEG C of steam after heat exchange is discharged from the steam port of heating coil (1-6), after discharge The recyclable recycling of steam.
14. the method according to claim 13 for producing coal-tar gas, it is characterised in that the step (2) is specifically：
(2.1) temperature is the fluidisation gas entry of 480~550 DEG C of bottom of the circulating gas through fluidized bed pyrolysis reactor (4) (4f) enters in reactor shell (4-1) from bottom to top, through step (1) dried dry coal through fluidized bed pyrolysis reactor (4) Dry coal entrance (4g) enter in reactor shell (4-1), in fluidisation heat exchange bed (4-2) with multi-cyclone (4-5) High temperature raw coke oven gas fluidisation heat exchange after dedusting, makes dry coal be heated to 360~380 DEG C, meanwhile, the heavy molecules analysis in raw coke oven gas Dry coal surface, fine dust is attached to after going out also to be swept along on dry coal surface as dry coal is through one-level overflow ducts (4-4) entrance warm Solve chamber；
(2.2) in chamber is pyrolyzed, the collected dry coal fine powder of dedusting combination enters fluid bed heat from dry coal fine powder charging aperture (4b) Mixed in solution reactor (4) with the dry coal after the heating of step (2.1), then 750~850 DEG C come with semicoke expansion chamber (7) High-temperature semi-coke mixes, and further fluidisation pyrolysis, and pyrolysis temperature is 480~650 DEG C, and raw coke oven gas caused by pyrolysis is with from reaction The fluidisation coal gas of device cylinder (4-1) is from bottom to top through multi-cyclone (4-5) dedusting, and after fluidisation heat exchange bed (4-2) Cool dedusting, is discharged afterwards by the raw coke oven gas export mouth (4a) at the top of reactor shell (4-1)；
(2.3) caused semicoke enters soot blowing separation bed (4-9) with two level overflow ducts (4-8) after being pyrolyzed, from fluidizing coal gas Air-flow drives dust to realize soot blowing to the circulating gas that entrance (4f) enters in flow process from bottom to top, the high-temperature semi-coke after soot blowing Filtrate into cross-current type granular-bed filter (12) as filter；And led from the raw coke oven gas at the top of reactor shell (4-1) Outlet (4a) discharge raw coke oven gas passes through cross-current type granular-bed filter (12) further dust removal by filtration, and the raw coke oven gas after dedusting deoils Wash tower (14) and carry out Oil-gas Separation, the coal gas part after separation returns to high-temperature heat-exchanging (10) and carries out hot friendship as circulating gas Change, a part is used as coal gas output of products, and the coal tar isolated exports as tar product.
15. the method according to claim 14 for producing coal-tar gas, it is characterised in that the step (3) is specifically：
The semicoke of cross-current type granular-bed filter (12) after raw coke oven gas dedusting from bottom further to discharging, and and fluidized bed pyrolysis The Oil-gas Separation mix dust rear portion of reactor (4) discharge goes coke powder to cool down the warehousing that defocused after waste heat boiler (13) cools down Deposit, a part goes fluidized bed combustor (5) to produce solid thermal carriers with mixed flue gas mixed combustion, and fluidized bed combustion gas velocity is 0.5 ~5.0m/s, then heated riser (6) be further heated to 750~850 DEG C after enter semicoke expansion chamber (7), heater riser (6) 15~25m/s of gas velocity is managed, is got off into the coke powder in semicoke expansion chamber (7) is most of by free settling, through high-temperature semi-coke Charging aperture (4c) is back in fluidized bed pyrolysis reactor (4), and 750~850 containing fine dust DEG C high-temperature flue gas passes through simultaneously Enter afterburning chamber (9) after high-temperature flue gas cyclone separator group (8) dedusting, further burn combustible gas a small amount of in high-temperature flue gas Body and dust, the high-temperature flue gas of afterburning chamber (9) discharge remove high-temperature heat-exchanging (10).
16. the method according to claim 15 for producing coal-tar gas, it is characterised in that the step (4) is specifically：
From afterburning chamber (9) discharge high-temperature flue gas in high-temperature heat-exchanging (10) with the part after air and step (1) dedusting The part coal gas that flue gas, the oil scrubber (14) of step (2) separate carries out heat exchange, obtains the low-heat cigarette that temperature is 300~380 DEG C Gas, 480~550 DEG C of circulating gas, the circulating flue gas that temperature is 450~550 DEG C and air that temperature is 450~550 DEG C； Temperature is that 300~380 DEG C of low-heat flue gas is done after desulphurization denitration is handled into multistage fluidized bed drier (1) to fine coal It is dry；The circulating gas that temperature is 480~550 DEG C enter from the bottom of fluidized bed pyrolysis reactor (4) and further fluidisation pyrolysis； Feeding fluidized bed combustor (5) enters one after the circulating flue gas for 450~550 DEG C of air and the temperature that temperature is 450~550 DEG C mixes Step burning, makes material reuse, waste heat recovery.
CN201710831382.6A 2017-09-15 2017-09-15 The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling Active CN107723012B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710831382.6A CN107723012B (en) 2017-09-15 2017-09-15 The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710831382.6A CN107723012B (en) 2017-09-15 2017-09-15 The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling

Publications (2)

Publication Number Publication Date
CN107723012A true CN107723012A (en) 2018-02-23
CN107723012B CN107723012B (en) 2019-08-23

Family

ID=61206301

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710831382.6A Active CN107723012B (en) 2017-09-15 2017-09-15 The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling

Country Status (1)

Country Link
CN (1) CN107723012B (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114717017A (en) * 2022-05-09 2022-07-08 孙孝德 Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal
CN114846123A (en) * 2019-12-27 2022-08-02 荏原环境工程株式会社 Thermal decomposition apparatus and thermal decomposition method
CN116286067B (en) * 2023-02-01 2024-03-15 四川大学 Long-period stable operation method and device for producing gasoline and diesel oil by biomass

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2428546A1 (en) * 2009-04-30 2012-03-14 Universidad De Concepcion Equipment and a method for generating biofuel based on rapid pyrolysis of biomass
CN203065402U (en) * 2013-03-06 2013-07-17 中煤能源黑龙江煤化工有限公司 Pulverized coal destructive distillation device
CN104178227A (en) * 2013-05-23 2014-12-03 中石化洛阳工程有限公司 Fluidized bed destructive distillation method and device of pulverized coal
CN106753491A (en) * 2017-01-17 2017-05-31 王树宽 A kind of solid thermal carriers activation coal gas flashing speed oven coal produces the system and method for coal tar, coal gas and semicoke

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2428546A1 (en) * 2009-04-30 2012-03-14 Universidad De Concepcion Equipment and a method for generating biofuel based on rapid pyrolysis of biomass
CN203065402U (en) * 2013-03-06 2013-07-17 中煤能源黑龙江煤化工有限公司 Pulverized coal destructive distillation device
CN104178227A (en) * 2013-05-23 2014-12-03 中石化洛阳工程有限公司 Fluidized bed destructive distillation method and device of pulverized coal
CN106753491A (en) * 2017-01-17 2017-05-31 王树宽 A kind of solid thermal carriers activation coal gas flashing speed oven coal produces the system and method for coal tar, coal gas and semicoke

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114846123A (en) * 2019-12-27 2022-08-02 荏原环境工程株式会社 Thermal decomposition apparatus and thermal decomposition method
CN114717017A (en) * 2022-05-09 2022-07-08 孙孝德 Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal
CN114717017B (en) * 2022-05-09 2022-12-06 孙孝德 Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal
CN116286067B (en) * 2023-02-01 2024-03-15 四川大学 Long-period stable operation method and device for producing gasoline and diesel oil by biomass

Also Published As

Publication number Publication date
CN107723012B (en) 2019-08-23

Similar Documents

Publication Publication Date Title
CN105219417B (en) Biomass pyrolysis system and biomass pyrolysis method
CN106753491B (en) System and method for preparing coal tar, coal gas and semicoke by activating coal gas through solid heat carrier and performing flash pyrolysis on coal
CN104449782B (en) Pyrolysis dust removal system and pyrolysis dust removal method based on coupling of small-size coal pyrolysis and raw gas dust removal
CN102643703B (en) Novel external heating type lignite pyrolysis quality increasing system and process
CN107723012B (en) The system and method for coal-tar gas is produced in multistage fluidized bed pulverized coal pyrolysis and dedusting coupling
CN106811220A (en) A kind of pyrolytic reaction separator and pyrolytic reaction separation method
CN109847657B (en) Fused salt heat supply fluidized bed pyrolysis reaction furnace and reaction method
CN104449774A (en) Down-flow gas semi-coke activated pulverized coal pyrolysis system and method
CN107267180A (en) Fine coal low-temperature rapid thermal solution system and technique
CN105778945B (en) It is pyrolyzed the system and method for biomass
CN107760344B (en) System and method for preparing coal tar gas by coupling pulverized coal pyrolysis and dust removal
CN109628121B (en) System and method for graded co-production of energy chemicals and silicon-carbon materials from rice husks
CN104593026B (en) A kind of scale low order fine coal low temperature pyrogenation device and method
CN112625720B (en) Cross-flow type coal mixing pyrolysis method and pyrolysis device
CN105885897B (en) A kind of pulverized coal pyrolysis dust pelletizing system of built-in grain bed and cyclone dust collectors
CN1175085C (en) Biomass integrated thermocracking equipment for preparing liquid fuel
CN205974378U (en) Fine coal pyrolysis dust pelletizing system of built -in cyclone and circulating grain bed
CN105802648B (en) Fine coal fast pyrolysis systems
CN105176547B (en) A kind of coal fast pyrolysis process
CN205838921U (en) Fine coal rapid pyrolysis apparatus
CN204417407U (en) A kind of mass-producing low order fine coal low temperature pyrogenation device
CN105670665B (en) Pulverized coal pyrolysis device
CN205653407U (en) Coal pyrolysis system
CN202610207U (en) Novel external-heated type brown coal pyrolysis quality-improving system
CN105907407A (en) Biomass pyrolysis system and method

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant