CN105950195A - Cocurrent downward circulating fluidized bed millisecond pyrolysis and liquefaction technology for biomass - Google Patents

Cocurrent downward circulating fluidized bed millisecond pyrolysis and liquefaction technology for biomass Download PDF

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Publication number
CN105950195A
CN105950195A CN201610565551.1A CN201610565551A CN105950195A CN 105950195 A CN105950195 A CN 105950195A CN 201610565551 A CN201610565551 A CN 201610565551A CN 105950195 A CN105950195 A CN 105950195A
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China
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gas
biomass
pyrolysis
flue gas
temperature
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CN201610565551.1A
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Chinese (zh)
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田原宇
乔英云
谢克昌
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China University of Petroleum East China
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China University of Petroleum East China
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Priority to CN201610565551.1A priority Critical patent/CN105950195A/en
Publication of CN105950195A publication Critical patent/CN105950195A/en
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    • 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
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D1/00—Fertilisers containing potassium
    • 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
    • C10B49/16—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 moving solid heat-carriers in divided form
    • 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
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Abstract

The invention provides a cocurrent downward circulating fluidized bed millisecond pyrolysis and liquefaction technology for biomass. Biomass powder is dried and lifted by a flue gas lifting pipe and subjected to gas-solid fractional separation at the top, flue gas is exhausted out, fine particles enter a semi-coke refeeder, large and medium particles achieve rapid mixed temperature increasing and millisecond pyrolysis with high-temperature circulating carriers at the top end of a downward pyrolysis reactor, and oil gas, heat carriers and semi-coke are quickly separated on the lower portion of a vertical pipe of the reactor; oils with different fractions and dry gas are obtained from pyrolysis oil gas through a fractionating tower, and the heat carriers and part of the semi-coke enter a coke burning lifting pipe to be burnt and heated; after the burnt high-temperature carriers are separated from the flue gas through two stages of gas-solid separators, the flue gas is subjected to heat exchange and then introduced to the bottom of the flue gas lifting pipe to lift and dry the biomass powder, large and medium particle carriers enter the top of the downward pyrolysis reactor to serve as the high-temperature circulating heat carriers, and fine ash enters a cooling stock bin and then is discharged to serve as silicon-potash fertilizer.

Description

Biomass downlink cycle bed millisecond pyrolysis liquefaction technique
1. technical field
The present invention provides biomass downlink cycle bed millisecond pyrolysis liquefaction technique, belongs to biomass energy source domain.
2. background technology
At present China's agriculture and forestry organic waste material more than about 8.8 hundred million tons, effectively utilize technology and having to be incinerated owing to lacking or Discarded, not only waste resource, also result in a large amount of society such as haze weather, atmospheric pollution, soil mineralization, fire and vehicle accident warp Ji and ecological problem, become focus and the difficult point of public attention.Existing biomass comprehensive utilization ways is quite wide, and a lot of approach provide Source utilization rate and economic benefit are the highest, such as papermaking, direct combustion power generation, cellulose ethanol and biogas etc., but due to scale and consumption Little, service efficiency is low, pollute or the requirement of specific region, all can not fundamentally meet the efficient high-valued cleaning of biomass scale Requirement.The fast pyrogenation refinement technique newly risen for nearly 30 years converts biomass into that energy density is big, be prone to storage and fortune Defeated liquid, can produce vehicle alternative fuel, liquid fuel and industrial chemicals, is that environment friendly, most promising oil replace , there is not product scale in Dai Pin and consumption region limits, it is possible to meets wanting of extensive, efficient, high-valued and cleanliness without any pollution Ask, be acknowledged as " technology that this century, bioenergy had most industrialization development potentiality ", be Bioenergy Exploitation the most in the world Emphasis and focus, be again the forward position quest projects of China's strategy new industry-new energy field.
Representative processes mainly has the rotation conical reaction process of Dutch Twente university, U.S.'s Georgia work in the world Bed reaction technique, Canada the bubbling Circulating Fluidized Bed Process of Ensyn IEEE, National Renewable carry in institute National Renewable Energy Laboratory (NREL) vortex reaction process, the multi-layer vacuum pyrolysis mill reaction process etc. of Laval University, Canada.Domestic respectively Unit develops similar techniques the most in succession.But due to defective workmanship and deficiency, current only rotating cone technique, bubbling are ciculation fluidized Bed process achieves ton industrialized production.In above-mentioned technique, only circulating fluidized bed fast pyrolysis process utilizes pyrolysis The heat that the part semicoke circulating combustion produced produces can meet the demand of reaction institute calorific requirement, reasonable energy utilization, liquid Yield is high, equipment simple, be prone to maximize, also studied both at home and abroad at most it is considered to be most possibly realize industrialization The biomass fast pyrogenation technique produced.But general recirculating fluidized bed pyrolysis needs fluidized gas, cooling load big, and fluidisation abrasion is produced Raw fine powder oil is difficult to remove.When downlink cycle fluid bed has the motion of suitable gravitational field cocurrent flow descending, solid solid or gas-solid contact Between short, reaction is fast, radial distribution is uniform, back-mixing is little and it is solid/gas to regulate neatly or solid than etc. advantage, both maintained fluidisation Bed is pyrolyzed to obtain high liquid yield and large-scale production advantage, again without fluidized wind, the pyrolysis gas time of staying is little, abrasion of particles is thin Powder is few, reduces cooling load and energy consumption, and in oil, deliming is relatively easy, thus downlink cycle fluid bed will be biomass Rapid Thermal The optimum response device of solution urgently development and application.But owing to biomass material is higher containing potassium, water content, simultaneously biomass material with And pyrolysis char and carrier difference of specific gravity are big, in the most typical fast pyrolysis process, generally exist Mass and heat transfer with Band ash in response regulatory, oil, High water cut in oil, liquid yield are low, oil gas coking and blocking, semicoke carrier different return to material, bio oil adds Hot autohemagglutination, fluidized gas dilute dry gas and power consumption, cause the dead bed of bed coking, biomass material to be dried, react containing potassium carrier is melted It is ten big that device mechanical moving element high temperature wear etc. affects biomass fast pyrogenation skilled industry amplification and long-period stable operation A difficult problem.
The present inventor has invented a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process (ZL200810000615.9), it is characterised in that the solid organic matters after drying and crushing is through delivering into certainly by conveying worm The entrance of mixing downflow fluidized bed reactor, with the high temperature regeneration agent entered from another entrance in self-mixing downflow fluidized bed reaction Device contacts, mix, react, quickly leave conversion zone；Gas phase is entered by the gaseous phase outlet of self-mixing downflow fluidized bed reactor Entering quencher condensation separation is pyrolysis oil and pyrolysis gas, separates through oil tank, and partial thermal decomposition oil is returned water-cooled by liquid circulation pump As quencher low-temperature receiver after device cooling；Solid phase enters fluid bed regenerator together with preheated air by material returning apparatus of fluidized bed and burns Regeneration, the solid temperature after fluidized bed regeneration raises, and enters inertia gas-solid separator, first separates major part granular solids and enters Regenerative agent surge bunker, enters back into self-mixing downflow fluidized bed reactor and again circulates, and remaining small solid is introduced into province with air-flow Coal device preheated air, separates subsequently into cyclone separator and arranges outside microparticle high-temp solid；Flue gas after separation is added by pulverizing Glassware enters the dry lifter of Organic substance dried bean noodles, then empties through air-introduced machine after dry Organic substance isolated by cyclone separator；Air Enter economizer through aerator and preheat laggard fluidized bed regenerator；Organic substance is dry by pulverizing feeder entrance Organic substance dried bean noodles Lifter, then delivers into the entrance of self-mixing downflow fluidized bed reactor through cyclone separator separation by conveying worm, this Sample is descending to be coupled from mixed fluidized bed reactor and fluid bed regenerator, forms the reaction regeneration coupling of a solid thermal carriers circulation Assembly system, it is achieved that Mass and heat transfer and the regulation and control of reaction.Although by heat carrier fractionated, under big-and-middle granule heat carrier passes through Arrange outside the pyrolysis of row pyrolysis reactor, molecule heat ash, from source, eliminate a band ash difficult problem in the oil that hot ash causes.But biomass The dried non-fractionated of powder, fine particle therein also can produce band ash phenomenon in oil from source.Oil gas is the most directly carried out Fractional distillation, in oil, High water cut problem fails effectively to solve.Additionally oil gas coking and blocking, semicoke carrier are different returns to material, bio oil heating The difficult problem that is dried autohemagglutination and biomass material perplexs the industrialization of biomass self-mixing downflow fluidized bed rapid pyrolysis process always and pushes away Extensively.
3. summary of the invention
The purpose of the present invention is contemplated to overcome the deficiency that existing biomass pyrolysis liquefaction technology exists and the one proposed Biomass downlink cycle bed millisecond pyrolysis liquefaction technique, the most thoroughly solves biomass pyrolytic Mass and heat transfer and response regulatory, oil Middle band ash, High water cut in oil, liquid yield are low, oil gas coking and blocking, semicoke carrier different return to material, bio oil heats autohemagglutination, fluidisation Gas dilution dry gas and power consumption, melted cause the dead bed of bed coking, biomass material to be dried containing potassium carrier, reactor mechanical movement portion Part high temperature wear etc. affects ten hang-ups of biomass fast pyrogenation skilled industry amplification and long-period stable operation.
Technical scheme:
It is an object of the invention to by biomass powder and heat carrier are all realized fractionated, big-and-middle particulate vector and biology Matter is pyrolyzed by descending pyrolysis reactor, biomass fine powder is sent directly into and burns riser combustion heating, thin heat carrier directly outside Row does Si-K fertilizer, eliminates band ash and biomass ash in oil and utilize and cause the dead bed of bed coking containing potassium carrier is melted from source A difficult problem.It is characterized in that the biomass powder being less than 6mm in a large number is dried through flue gas riser and is promoted, biomass powder is by two grades of gas Solid separator fractionated, arranges outside flue gas, and fine grained biomass are entered by semicoke returning charge valve burns riser, and big-and-middle granule is raw The rotated feeder of material is at descending pyrolysis reactor top and the high temperature circulation heat carrier fallen by higher temperature carrier returning charge valve Realize rapidly quickly mixing to heat up and millisecond is pyrolyzed, at reactor standpipe bottom oil gas and semicoke and heat carrier at gas-solid separator The lower sharp separation of effect；Pyrolysis oil gas is fractionated into tower and obtains different fractions oil product and dry gas, heat carrier and part semicoke by sky The semicoke returning charge valve of gas conveying enters and burns riser combustion heating, and part semicoke flows into external warmer and takes conduct half after heat drop temperature Burnt product；Higher temperature carrier after burning is after two-stage gas-solid separator separates with flue gas, and flue gas is introduced to flue gas after heat exchange Promoting and dried biomass powder bottom riser, big-and-middle granule heat carrier enters descending pyrolysis reactor top as high temperature circulation Heat carrier, fine ash is outer after entering cooling feed bin arranges as Si-K fertilizer.
Burning riser reaction temperature is 850 DEG C-1100 DEG C.
High-temperature heat carrier is 2-8:1 with the mixed proportion of biomass powder.
Descending pyrolysis reactor outlet reaction temperature is 450 DEG C-600 DEG C.
External warmer can be to utilize dry gas that semicoke heat exchange in fluidisation state external warmer of 450 DEG C-600 DEG C is produced height Pressure steam, the separated device of dry gas reclaims is intake by water inlet preheater preheating external warmer after solid particle, be cooled to 300 DEG C with Under, utilize circulating fan to send into bottom fluidisation state external warmer, half afocal row's temperature is less than 260 DEG C.
Embodiment is described the feature of the present invention by the present invention in detail.
4. accompanying drawing explanation
Accompanying drawing is the process schematic representation of the present invention.The drawing of accompanying drawing sets bright as follows:
1, riser 2, gas distributor 3, air inlet pipe 4, inertia gas-solid separator 5, higher temperature carrier returning charge control are burnt Device 6 processed, two grades of gas-solid separators 7 of heat carrier, fine ash cooling feed bin 8, descending pyrolysis reactor 9, oil gas gas-solid separator 10, oil gas fractionating column 11, heavy oil outlet 12, light oil outlet 13, wood vinegar outlet 14, air-introduced machine 15, flue gas riser 16, flue gas one-level gas-solid separator 17, top feed bin 18, rotary table feeder 19, flue gas two grades of gas-solid separators 20, flue gases Outlet 21, biomass powder entrance 22, dry gas outlet 23, semicoke returning charge valve 24, fluidisation state external warmer 25, separator 26, water inlet preheater 27, circulating fan 28, semicoke separator 29, semicoke outlet.
The process characteristic of the present invention is described in detail in detail with embodiment below in conjunction with the accompanying drawings.
5. detailed description of the invention
Embodiment, by biomass powder less than 6mm in a large number through biomass powder entrance 21 enter flue gas riser 15 be dried and Promoting, biological particles is by flue gas one-level gas-solid separator 16 and two grades of gas-solid separator 19 fractionated of flue gas, and flue gas is from cigarette The outer row of gas outlet 20, fine grained biomass are entered by semicoke returning charge valve 23 burns riser 1, and big-and-middle grain biomass is rotated Feeder 18 is real rapidly with the high temperature circulation heat carrier fallen by higher temperature carrier returning charge valve 5 on descending pyrolysis reactor 8 top Now quickly mix and heat up and millisecond pyrolysis, grey with semicoke and heat in oil gas gas-solid at descending pyrolysis reactor 8 standpipe bottom oil gas The lower sharp separation of separator 9 effect, heat carrier and part semicoke are entered by the semicoke returning charge valve 23 that air carries and burn lifting Pipe 1 mixes with the air of air inlet pipe 3 and gas distributor 2, combustion heating；Oil gas containing semicoke is again through semicoke separator 28 gas solid separation, semicoke flows into fluidisation state external warmer 24 dry gas heat exchange cooling, and the semicoke after cooling goes out from semicoke as product Mouth 29 is discharged；Pyrolysis oil gas is fractionated into tower 10 and obtains wood vinegar 13, light oil 12, heavy oil 11 and pyrolysis dry gas 22；Height after heating Warm carrier is after two grades of gas-solid separators 6 of inertia gas-solid separator 4 and heat carrier separate with flue gas, and flue gas is through waste heat boiler After heat exchange by air-introduced machine 14 guide to promote bottom flue gas riser 15 and be dried from biomass powder entrance 21 add less than 6mm's Biomass powder, big-and-middle granule heat carrier enters descending pyrolysis reactor 8 top as high temperature circulation carrier, fine ash entrance cooling material Behind storehouse 7, outer row is as Si-K fertilizer
Burning riser 1 reaction temperature is 850 DEG C-1100 DEG C.
High-temperature heat carrier is 2-8:1 with the mixed proportion of biomass powder.
It is 450 DEG C-600 DEG C that descending pyrolysis reactor 8 exports reaction temperature.
External warmer 24 can be to utilize dry gas by raw for semicoke heat exchange in fluidisation state external warmer 24 of 450 DEG C-600 DEG C Producing high steam, the separated device of dry gas 25 preheats external warmer 24 by water inlet preheater 26 after reclaiming solid particle and intakes, cold But to less than 300 DEG C, utilizing circulating fan 27 to send into bottom fluidisation state external warmer 24, half afocal row's temperature is less than 260 DEG C.
Biomass downlink cycle bed millisecond pyrolysis liquefaction technique provided by the present invention, by by biomass powder and heat carrier All realize that fractionated, big-and-middle particulate vector and biomass are pyrolyzed by descending pyrolysis reactor, biomass fine powder is sent directly into Burning riser combustion heating, thin heat carrier directly outer row does Si-K fertilizer, and from source, in elimination oil, band ash, fluidized gas dilute dry Gas and power consumption and biomass ash utilize and melt, containing potassium carrier, the difficult problem causing the dead bed of bed coking.Utilize and burn riser High gas velocity, the freely falling body of down pipe and semicoke material returning device eliminate that semicoke carrier is different returns to a material difficult problem；Utilize two-tube (descending Reaction tube and burn riser) coupling solves regulation and control and the reactor mechanical moving element high temperature wear of Mass and heat transfer and reaction A difficult problem；Oil and gas straight fractional distillation is utilized to solve a High water cut difficult problem in oil gas coking and blocking and bio oil heating autohemagglutination and oil； Utilize flue gas drying biomass, solve biomass material and be dried a difficult problem, improve pyrolysis heating rate thus improve liquid Yield, these technical measures integrated, thus solve and affect biomass fast pyrogenation skilled industry amplification and long period is stable Ten hang-ups run, eliminate the bottleneck of puzzlement biomass self-mixing downflow fluidized bed rapid pyrolysis process industrialization promotion. The liquid yield of different biomass fast pyrogenations: pine powder 68%, Poplar Powder 62%, corn straw 39%, cotton stalk 55%, Containing ash less than 0.2% in oil, aqueous it is less than 1%；Gas heating value about 3800 kilocalorie, semicoke calorific value about 5400 kilocalorie.

Claims (5)

1. biomass downlink cycle bed millisecond pyrolysis liquefaction technique, is characterized in that being less than the biomass powder of 6mm in a large number through flue gas Riser is dried and promotes, and biomass powder, by two grades of gas-solid separator fractionated, is arranged outside flue gas, and fine grained biomass are by half Burnt returning charge valve enters and burns riser, and the rotated feeder of big-and-middle grain biomass is on descending pyrolysis reactor top and by height The high temperature circulation heat carrier that temperature carrier returning charge valve falls realizes rapidly quickly mixing intensification and is pyrolyzed with millisecond, under reactor standpipe Portion's oil gas and semicoke and heat carrier sharp separation under gas-solid separator effect；Pyrolysis oil gas is fractionated into tower and obtains different fractions oil Product and dry gas, heat carrier and part semicoke are entered by the semicoke returning charge valve that air carries and burn riser combustion heating, part Semicoke flows into external warmer and takes after heat drop temperature as semicoke product；Higher temperature carrier after burning is through two-stage gas-solid separator and flue gas After separation, flue gas is introduced to bottom flue gas riser promote and dried biomass powder after heat exchange, and big-and-middle granule heat carrier enters Enter descending pyrolysis reactor top to arrange as Si-K fertilizer outward after cooling down feed bin as high temperature circulation heat carrier, fine ash entrance.
Biomass downlink cycle bed millisecond pyrolysis liquefaction technique the most according to claim 1, it is characterised in that burn lifting Tube reaction temperature is 850 DEG C-1100 DEG C.
Biomass downlink cycle bed millisecond pyrolysis liquefaction technique the most according to claim 1, it is characterised in that high-temperature hot carries Body is 2-8:1 with the mixed proportion of biomass powder.
Biomass downlink cycle bed millisecond pyrolysis liquefaction technique the most according to claim 1, it is characterised in that descending pyrolysis Reactor outlet reaction temperature is 450 DEG C-600 DEG C.
Biomass downlink cycle bed millisecond pyrolysis liquefaction technique the most according to claim 1, it is characterised in that external warmer Can be to utilize dry gas that semicoke heat exchange in fluidisation state external warmer of 450 DEG C-600 DEG C is produced high steam, dry gas be through dividing Intake by water inlet preheater preheating external warmer after device reclaims solid particle, be cooled to less than 300 DEG C, utilize circulating fan Sending into bottom fluidisation state external warmer, half afocal row's temperature is less than 260 DEG C.
CN201610565551.1A 2016-07-18 2016-07-18 Cocurrent downward circulating fluidized bed millisecond pyrolysis and liquefaction technology for biomass Withdrawn CN105950195A (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106939171A (en) * 2017-03-22 2017-07-11 中国石油大学(华东) Biomass downlink cycle bed millisecond pyrolysis liquefaction technique
CN107723014A (en) * 2017-10-25 2018-02-23 浙江科技学院 A kind of biomass fast pyrogenation upgrading purifier and technique
CN108192647A (en) * 2018-01-04 2018-06-22 山西新唐工程设计股份有限公司 A kind of low energy consumption pulverized coal pyrolysis technique
CN110066667A (en) * 2019-04-11 2019-07-30 嘉禾聚能（天津）科技有限公司 The vertical pyrolysis reactor and pyrolytic reaction system of solid thermal carriers circulation
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

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106939171A (en) * 2017-03-22 2017-07-11 中国石油大学(华东) Biomass downlink cycle bed millisecond pyrolysis liquefaction technique
CN107723014A (en) * 2017-10-25 2018-02-23 浙江科技学院 A kind of biomass fast pyrogenation upgrading purifier and technique
CN107723014B (en) * 2017-10-25 2023-03-10 浙江科技学院 Biomass fast pyrolysis quality improvement purification device and process
CN108192647A (en) * 2018-01-04 2018-06-22 山西新唐工程设计股份有限公司 A kind of low energy consumption pulverized coal pyrolysis technique
CN110066667A (en) * 2019-04-11 2019-07-30 嘉禾聚能（天津）科技有限公司 The vertical pyrolysis reactor and pyrolytic reaction system of solid thermal carriers circulation
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

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Application publication date: 20160921