CN106800941A - Biomass downlink cycle bed millisecond pyrolysis liquefaction device - Google Patents
Biomass downlink cycle bed millisecond pyrolysis liquefaction device Download PDFInfo
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- CN106800941A CN106800941A CN201710171662.9A CN201710171662A CN106800941A CN 106800941 A CN106800941 A CN 106800941A CN 201710171662 A CN201710171662 A CN 201710171662A CN 106800941 A CN106800941 A CN 106800941A
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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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides biomass downlink cycle bed millisecond pyrolysis liquefaction device, biological powder entrance is arranged on flue gas riser bottom, flue gas riser top sets gas-solid second-stage separator, and primary separator solid outlet is connected by top feed bin and rotary table feeder with descending pyrolysis reactor top；Second-stage separator exhanst gas outlet is directly outer to be arranged, and solid outlet is connected by semicoke returning charge valve with lifting bottom of the tube is burnt；Riser is burnt for bottom sets gas distributor and air inlet pipe, and top is set inertia separator and connected with descending pyrolysis reactor top by carrier returning charge controller；Heat carrier separator solid outlet cools down feed bin with fine ash, and gaseous phase outlet lifts bottom of the tube and connects by air-introduced machine and flue gas；Descending pyrolysis reactor bottom sets gs-oil separator and semicoke separator, and gs-oil separator bottom is connected by semicoke returning charge valve with lifting bottom of the tube is burnt；Semicoke separator solid outlet is connected with fluidisation state external warmer, and semicoke separator gaseous phase outlet is connected with oil gas fractionating column.
Description
1. technical field
The present invention provides biomass downlink cycle bed millisecond pyrolysis liquefaction device, belongs to biomass energy source domain.
2. background technology
More than about 8.8 hundred million tons of current China's agriculture and forestry organic waste material, effectively have to be incinerated using technology due to lacking or
Discarded, not only waste of resource, also results in a large amount of society's warps such as haze weather, atmosphere pollution, soil mineralization, fire and traffic accident
Ji and ecological problem, focus and difficult point as public attention.Existing biomass comprehensive utilization ways are quite wide, many approach moneys
Source utilization rate and economic benefit are all very high, such as papermaking, direct combustion power generation, cellulose ethanol and biogas, but due to scale and consumption
Small, service efficiency is low, pollution or specific region are required, all can not fundamentally meet biomass scale efficiently high-valued cleaning
Requirement.Nearly 30 years new fast pyrogenation refinement techniques for rising convert biomass into that energy density is big, are easy to store and transport
Defeated liquid, can produce vehicle alternative fuel, liquid fuel and industrial chemicals, be that environment friendly, most promising oil are replaced
Dai Pin, in the absence of product scale and consumption territory restriction, disclosure satisfy that extensive, efficient, high-valued and cleanliness without any pollution wanting
Ask, be acknowledged as " technology that this century biological energy source most there are industrialization development potentiality ", be both current Bioenergy Exploitation in the world
Emphasis and focus, be again China strategy new industry-new energy field forward position quest projects.
Representative processes mainly have the rotation conical reaction process of Dutch Twente universities, U.S.'s Georgia works in the world
Institute carries bed reaction technique, bubbling Circulating Fluidized Bed Process, the National Renewable of Ensyn IEEEs of Canada
National Renewable Energy Laboratory (NREL) vortex reaction process, multi-layer vacuum pyrolysis mill reaction process of Laval University, Canada etc..It is domestic each
Unit also develops similar techniques in succession.But due to defective workmanship and deficiency, only rotating cone technique, bubbling are ciculation fluidized at present
Bed process realizes ton industrialized production.In above-mentioned technique, only circulating fluidized bed fast pyrolysis process is using pyrolysis
The heat that the part semicoke circulating combustion of generation is produced can meet the demand of reaction institute calorific requirement, reasonable energy utilization, liquid
High income, equipment are simple, be easy to maximize, be also studied both at home and abroad most, it is considered to be it is most possible to realize industrialization
The biomass fast pyrogenation technique of production.But general recirculating fluidized bed pyrolysis needs fluidized gas, cooling load big, fluidizes abrasion and produces
It is difficult to remove in raw fine powder oil.When downlink cycle fluid bed has along the motion of gravitational field cocurrent flow descending, solid or gas-solid contact
Between it is short, reaction is fast, radial distribution is uniform, back-mixing is small and it is solid/gas neatly to adjust or it is solid than the advantages of, both maintained fluidisation
Bed is pyrolyzed to obtain liquid yield high and large-scale production advantage, and without fluidized wind, pyrolysis gas residence time be small, abrasion of particles is thin
Powder is few, reduces cooling load and energy consumption, and deliming is relatively easy in oil, thus downlink cycle fluid bed will be the fast speed heat of biomass
The optimum response device of solution urgently development and application.But because biomass material is higher containing potassium, water content, at the same biomass material with
And pyrolysis char and carrier difference of specific gravity are big, at present in the world in typical fast pyrolysis process, generally existing Mass and heat transfer with
High water cut, low liquid yield, oil gas coking and blocking, the different material, bio oil of returning to of semicoke carrier add in band ash, oil in response regulatory, oil
Hot autohemagglutination, fluidized gas dilution dry gas and power consumption, the melting containing potassium carrier cause the dead bed of bed coking, biomass material to dry, reaction
Device mechanical moving element high temperature wear etc. influences the ten big of biomass fast pyrogenation skilled industry amplification and long-period stable operation
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 are passed through and delivered 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
Contacted in device, mixed, reacted, quickly leave conversion zone；Gas phase is entered by the gaseous phase outlet of self-mixing downflow fluidized bed reactor
Enter quencher condensation separation for pyrolysis oil and pyrolysis gas, separated through oil tank, partial thermal decomposition oil returns water-cooled by liquid circulation pump
As quencher low-temperature receiver after device cooling；Solid phase is entered fluid bed regenerator by material returning apparatus of fluidized bed and preheated air and burnt together
Regeneration, raises through the solid temperature after fluidized bed regeneration, into inertia gas-solid separator, first separates most of granular solids and enters
Regenerative agent surge bunker, enters back into self-mixing downflow fluidized bed reactor and circulates again, and remaining small solid is introduced into province with air-flow
Coal device preheated air, separates subsequently into cyclone separator and arranged outside microparticle high-temp solid；Flue gas after separation is added by crushing
Glassware enters the dry lifter of organic matter dried bean noodles, is emptied through air-introduced machine after then isolating dry organic matter through cyclone separator；Air
Enter economizer through air blower and preheat laggard fluidized bed regenerator；Organic matter is dry into organic matter dried bean noodles by crushing feeder
Lifter, then separates the entrance that self-mixing downflow fluidized bed reactor is delivered into by conveying worm through cyclone separator, this
Sample is descending to be coupled from mixed fluidized bed reactor and fluid bed regenerator, forms a reaction regeneration coupling for solid thermal carriers circulation
Syzygy is united, and realizes the regulation and control of Mass and heat transfer and reaction.Although be classified by heat carrier separating, under big-and-middle particle heat carrier passes through
The pyrolysis of row pyrolysis reactor, the outer row of molecule heat ash, eliminate the grey problem of band in the oil that hot ash is caused from source.But biomass
Separation is not classified after dried bean noodles is dry, fine particle therein can also produce the grey phenomenon of band in oil from source.Oil gas is not carried out directly
Fractionation, High water cut problem fails effectively solution in oil.Other oil gas coking and blocking, semicoke carrier are different to return to material, bio oil heating
The industrialization that the problem that autohemagglutination and biomass material dries perplexs biomass self-mixing downflow fluidized bed rapid pyrolysis process always is pushed away
Extensively.
3. the content of the invention
The purpose of the present invention is exactly the one kind proposed to overcome the shortcomings of existing biomass pyrolysis liquefaction technology to exist
Biomass downlink cycle bed millisecond pyrolysis liquefaction device, had both thoroughly solved biomass pyrolytic Mass and heat transfer and response regulatory, oil
High water cut, low liquid yield, oil gas coking and blocking, semicoke carrier are different in middle band ash, oil returns to material, bio oil heating autohemagglutination, fluidisation
Gas dilutes dry gas and power consumption, the melting containing potassium carrier causes the dead bed of bed coking, biomass material drying, reactor mechanical movement portion
Part high temperature wear etc. influences ten hang-ups of biomass fast pyrogenation skilled industry amplification and long-period stable operation.
Technical scheme：
The purpose of the present invention is to realize classification separation, big-and-middle particulate vector and biology by by biomass powder and heat carrier
Matter is pyrolyzed by descending pyrolysis reactor, biomass fine powder is sent directly into and burns riser combustion heating, and thin heat carrier is directly outer
Row does Si-K fertilizer, and band ash and biomass ash are utilized and the melting containing potassium carrier causes the dead bed of bed coking in elimination oil from source
Problem.It is characterized in that biomass powder entrance is arranged on the bottom of flue gas riser, gas-solid two is set at the top of flue gas riser
Level separator, the exhanst gas outlet of one-level gas-solid separator is connected with two grades of gas-solid separator entrances, and one-level gas-solid separator is consolidated
Body outlet is connected by top feed bin and rotary table feeder with descending pyrolysis reactor top；The flue gas of two grades of gas-solid separators goes out
Mouthful directly outer row, two grades of solid outlets of gas-solid separator are connected by semicoke returning charge valve with lifting bottom of the tube is burnt；Burn and carry
Riser is that bottom sets gas distributor and air inlet pipe, and top sets inertia gas-solid separator；The solid of inertia gas-solid separator
Outlet is connected by higher temperature carrier returning charge controller with descending pyrolysis reactor top, and exhanst gas outlet divides with two grades of gas-solids of heat carrier
Entrance from device is communicated；Two grades of solid outlets of gas-solid separator of heat carrier cool down feed bin with fine ash, and gaseous phase outlet passes through air inducing
Machine is connected with the bottom of flue gas riser；Descending pyrolysis reactor bottom sets oil gas gas-solid separator, oil gas gas-solid separator
Gaseous phase outlet communicated with the entrance of semicoke separator, bottom by semicoke returning charge valve with burn lifting bottom of the tube connect；Semicoke
The solid outlet of separator is connected with external warmer, and the gaseous phase outlet of semicoke separator is connected with oil gas fractionating column.
Oil gas fractionating column sets desuperheating section and two sections of rectifying tower internals, and the outlet of pyrolysis dry gas, wooden vinegar are set from top to bottom
Liquid outlet, light oil outlet, heavy oil outlet.
External warmer is that fluidisation state external warmer bottom sets gas distributor, and top gas outlet passes through separator, enters
Water preheater and circulating fan are connected with the gas distributor of fluidisation state external warmer bottom.
Riser reaction temperature is burnt for 850 DEG C -1100 DEG C.
High-temperature heat carrier is 2-8 with the mixed proportion of biomass powder：1.
Descending pyrolysis reactor outlet reaction temperature is 450 DEG C -600 DEG C.
Embodiment is described the features of the present invention by the present invention in detail.
4. illustrate
Accompanying drawing 1 is process schematic representation of the invention.The drawing of accompanying drawing 1 sets bright as follows：
1st, riser 2, gas distributor 3, air inlet pipe 4, inertia gas-solid separator 5, higher temperature carrier returning charge control are burnt
Device processed 6, heat carrier two grades of gas-solid separator 7, fine ash cooling feed bins 8, descending pyrolysis reactor 9, oil gas gas-solid separators
10th, oil gas fractionating column 11, heavy oil outlet 12, light oil outlet 13, pyrolkigneous liquid outlet 14, air-introduced machine 15, flue gas riser
16th, flue gas one-level gas-solid separator 17, top feed bin 18, rotary table feeder 19, two grades of gas-solid separators 20, flue gas of flue gas
Outlet 21, biomass powder entrance 22, pyrolysis dry gas outlet 23, semicoke returning charge valve 24, external warmer 25, separator 26,
Enter water preheater 27, circulating fan 28, the outlet of semicoke separator 29, semicoke.
With reference to the accompanying drawings and examples in detail process characteristic of the invention is described in detail.
5. specific embodiment
Biomass powder entrance 21 is arranged on the bottom of flue gas riser 15, and two grades of gas-solid is set at the top of flue gas riser 15
Separator, the exhanst gas outlet of one-level gas-solid separator 16 is connected with two grades of entrances of gas-solid separator 19, one-level gas-solid separator 16
Solid outlet connected with the top of descending pyrolysis reactor 8 by top feed bin 17 and rotary table feeder 18；Two grades of gas solid separations
The exhanst gas outlet of device 19 is directly outer to be arranged, and two grades of solid outlets of gas-solid separator 19 are by semicoke returning charge valve 23 and burn riser
1 bottom connects；Riser 1 is burnt for bottom sets gas distributor 2 and air inlet pipe 3, and top sets inertia gas-solid separator 4；
The solid outlet of inertia gas-solid separator 4 is connected by higher temperature carrier returning charge controller 5 with the top of descending pyrolysis reactor 8, cigarette
Gas outlet is communicated with the entrance of two grades of gas-solid separators 6 of heat carrier；The solid outlet and fine ash of two grades of gas-solid separators 6 of heat carrier
Cooling feed bin 7, gaseous phase outlet is connected by air-introduced machine 14 with the bottom of flue gas riser 15；The bottom of descending pyrolysis reactor 8 sets
Oil gas gas-solid separator 9 is put, the gaseous phase outlet of oil gas gas-solid separator 9 is communicated with the entrance of semicoke separator 28, and bottom passes through
Semicoke returning charge valve 23 is connected with the bottom of riser 1 is burnt；The solid outlet of semicoke separator 28 connects with fluidisation state external warmer 24
Logical, the gaseous phase outlet of semicoke separator 25 is connected with oil gas fractionating column 10.
Oil gas fractionating column 10 set desuperheating section and two sections of rectifying tower internals, from top to bottom set pyrolysis dry gas outlet 22,
Pyrolkigneous liquid outlet 13, light oil outlet 12, heavy oil outlet 11.
External warmer 24 is that fluidisation state external warmer bottom sets gas distributor, and top gas outlet passes through separator
25th, enter water preheater 26 and circulating fan 27 to be connected with the gas distributor of fluidisation state external warmer bottom.
The reaction temperature of riser 1 is burnt for 850 DEG C -1100 DEG C.
High-temperature heat carrier is 2-8 with the mixed proportion of biomass powder：1.
The outlet reaction temperature of descending pyrolysis reactor 8 is 450 DEG C -600 DEG C.
Biomass downlink cycle provided by the present invention bed millisecond pyrolysis liquefaction device, by by biomass powder and heat carrier
Realize that classification is separated, big-and-middle particulate vector and biomass are pyrolyzed by descending pyrolysis reactor, biomass fine powder is sent directly into
Riser combustion heating is burnt, directly outer row does Si-K fertilizer to thin heat carrier, and band ash, fluidized gas dilution are done in elimination oil from source
Gas and power consumption and biomass ash cause the problem of the dead bed of bed coking using and containing potassium carrier melting.Using burning riser
High gas velocity, the freely falling body of down pipe and semicoke material returning device eliminate that semicoke carrier is different to return to material problem；Using two-tube (descending
Reaction tube and burn riser) coupling solve Mass and heat transfer with reaction regulation and control and reactor mechanical moving element high temperature wear
Problem；High water cut problem in solving oil gas coking and blocking and bio oil heating autohemagglutination and oil using oil and gas straight fractional distillation；
Using flue gas drying biomass, solve biomass material and dry problem, improve pyrolysis heating rate so as to improve liquid
Yield, these technical measures it is integrated, so as to solve influence biomass fast pyrogenation skilled industry amplification and long period stabilization
Ten hang-ups of operation, 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%, maize straw 39%, cotton
Stalk 55%, it is aqueous to be less than 1% containing ash less than 0.2% in oil；The kilocalorie of gas heating value about 3800, the kilocalorie of semicoke calorific value about 5400.
Claims (6)
1. biomass downlink cycle bed millisecond pyrolysis liquefaction device, it is characterized in that biomass powder entrance is arranged on flue gas riser
Bottom, sets gas-solid second-stage separator, the exhanst gas outlet of one-level gas-solid separator and two grades of gas-solids point at the top of flue gas riser
It is connected from device entrance, the solid outlet of one-level gas-solid separator passes through top feed bin and rotary table feeder and descending pyrolysis reactor
Top connects；Two grades of exhanst gas outlets of gas-solid separator are directly arranged outward, and the solid outlet of two grades of gas-solid separators is returned by semicoke
Material valve is connected with lifting bottom of the tube is burnt；Riser is burnt for bottom sets gas distributor and air inlet pipe, and top sets inertia
Gas-solid separator；The solid outlet of inertia gas-solid separator is by higher temperature carrier returning charge controller and descending pyrolysis reactor top
Connection, exhanst gas outlet is communicated with the entrance of two grades of gas-solid separators of heat carrier；Two grades of solid outlets of gas-solid separator of heat carrier
Feed bin is cooled down with fine ash, gaseous phase outlet is connected by air-introduced machine with the bottom of flue gas riser；Descending pyrolysis reactor bottom sets
Oil gas gas-solid separator is put, the gaseous phase outlet of oil gas gas-solid separator is communicated with the entrance of semicoke separator, bottom passes through semicoke
Returning charge valve is connected with lifting bottom of the tube is burnt；The solid outlet of semicoke separator is connected with fluidisation state external warmer, and semicoke is separated
The gaseous phase outlet of device is connected with oil gas fractionating column.
2. biomass downlink cycle according to claim 1 bed millisecond pyrolysis liquefaction device, it is characterised in that burn lifting
It is the alternate pulse pipe reactor of thickness to manage, and burns riser reaction temperature for 850 DEG C -1100 DEG C.
3. biomass downlink cycle according to claim 1 bed millisecond pyrolysis liquefaction device, it is characterised in that high warm is carried
Body is 2-8 with the mixed proportion of biomass powder：1.
4. biomass downlink cycle according to claim 1 bed millisecond pyrolysis liquefaction device, it is characterised in that descending pyrolysis
Reactor outlet reaction temperature is 450 DEG C -600 DEG C.
5. biomass downlink cycle according to claim 1 bed millisecond pyrolysis liquefaction device, it is characterised in that external warmer
It is that fluidisation state external warmer bottom sets gas distributor, top gas outlet passes through separator, enters water preheater and circulated air
Machine is connected with the gas distributor of fluidisation state external warmer bottom.
6. biomass downlink cycle according to claim 1 bed millisecond pyrolysis liquefaction device, it is characterised in that oil gas is fractionated
Tower setting desuperheating section and two sections of rectifying tower internals, setting pyrolysis dry gas is exported from top to bottom, pyrolkigneous liquid is exported, light oil is exported,
Heavy oil is exported.
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| CN201710171662.9A CN106800941A (en) | 2017-03-22 | 2017-03-22 | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
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| CN201710171662.9A CN106800941A (en) | 2017-03-22 | 2017-03-22 | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109593551A (en) * | 2018-11-02 | 2019-04-09 | 中国石油大学(华东) | For gas phase millisecond catalytic cracking integrated reaction and separation equipment |
| CN110396421A (en) * | 2019-08-19 | 2019-11-01 | 七台河宝泰隆新能源有限公司 | A kind of preventing mean and method of restructuring asphalt tower pipeline coking and blocking pipeline |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106190214A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
-
2017
- 2017-03-22 CN CN201710171662.9A patent/CN106800941A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106190214A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109593551A (en) * | 2018-11-02 | 2019-04-09 | 中国石油大学(华东) | For gas phase millisecond catalytic cracking integrated reaction and separation equipment |
| CN110396421A (en) * | 2019-08-19 | 2019-11-01 | 七台河宝泰隆新能源有限公司 | A kind of preventing mean and method of restructuring asphalt tower pipeline coking and blocking pipeline |
| CN110396421B (en) * | 2019-08-19 | 2024-02-02 | 七台河宝泰隆新能源有限公司 | Device and method for preventing coking and blockage of modified asphalt tower pipeline |
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