CN109628155A - Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device - Google Patents
Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device Download PDFInfo
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- CN109628155A CN109628155A CN201811501372.7A CN201811501372A CN109628155A CN 109628155 A CN109628155 A CN 109628155A CN 201811501372 A CN201811501372 A CN 201811501372A CN 109628155 A CN109628155 A CN 109628155A
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- 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
Abstract
The present invention provides biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device, biological powder entrance is arranged in hot-air riser lower part, gas-solid second-stage separator is set at the top of hot-air riser, and primary separator solid outlet at the top of top feed bin and rotary table feeder and downlink pyrolysis reactor by being connected to；The direct outlet of second-stage separator air outlet slit, solid outlet promote bottom of the tube with gasification by semicoke returning charge valve and are connected to；The riser that gasifies is that gas distributor and air inlet pipe is arranged in bottom, and top setting inertia separator at the top of carrier returning charge controller and downlink pyrolysis reactor by being connected to；Heat carrier separator solid outlet and the cooling feed bin of fine ash, gaseous phase outlet pass through water- to-water heat exchanger and air heat exchanger and dry gas outlet；Gs-oil separator is arranged in downlink pyrolysis reactor bottom, and gs-oil separator bottom promotes bottom of the tube with gasification by semicoke returning charge valve and is connected to, and gaseous phase outlet is connected with oil gas fractionating column；Air pressurized machine promotes bottom of the tube with hot-air all the way by air heat exchanger and is connected to, and the air inlet pipe for promoting bottom of the tube setting with gasification all the way is connected to；The air inlet pipe that water- to-water heat exchanger steam (vapor) outlet also promotes bottom of the tube setting with gasification is connected to.
Description
1. technical field
The present invention provides biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device, belongs to biomass energy neck
Domain.
2. background technique
About 8.8 hundred million tons of China's agriculture and forestry organic waste material or more at present, due to lack effective use technology and having to be incinerated 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, become the focus and difficult point of 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
It is small, service efficiency is low, pollution or specific region require, all cannot fundamentally meet the efficiently high-valued cleaning of biomass scale
Requirement.The nearly 30 years fast pyrogenation refinement techniques newly risen convert biomass into that energy density is big, is easy to store and transport
Defeated liquid can produce vehicle alternative fuel, liquid fuel and industrial chemicals, be that environment friendly, most promising petroleum replace
Dai Pin, there is no product scales and consumption territory restriction, can satisfy extensive, efficient, high-valued and cleanliness without any pollution want
It asks, is acknowledged as " technology that this century biological energy source most has industrialization development potentiality ", be both current Bioenergy Exploitation in the world
Emphasis and hot spot, and be China's strategy new industry-new energy field forward position quest projects.
Representative processes mainly have the rotation conical reaction process of Dutch Twente university, U.S.'s Georgia work in the world
Bubbling Circulating Fluidized Bed Process, the National Renewable for carrying bed reaction technique, Canada's Ensyn Association of Engineers of institute
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 10,000 tons industrialized production.In above-mentioned technique, only circulating fluidized bed fast pyrolysis process utilizes pyrolysis
The heat that the part semicoke circulating combustion of generation generates can meet the needs of reaction institute's calorific requirement, reasonable energy utilization, liquid
High income, equipment are simple, are easy to enlargement and are studied both at home and abroad most, it is considered to be most possible to realize industrialization
The biomass fast pyrogenation technique of production.But general recirculating fluidized bed pyrolysis needs fluidized gas, cooling load big, and fluidisation abrasion produces
It is difficult to remove in raw fine powder oil.When downlink cycle fluidized bed has along the movement 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 consolidate than the advantages that, both maintained fluidisation
Bed is pyrolyzed to obtain high liquid yield and large-scale production advantage, but without fluidized wind, the pyrolysis gas residence time is small, abrasion of particles is thin
Powder is few, reduces cooling load and energy consumption, deliming is relatively easy in oil, thus downlink cycle fluidized bed will be the fast speed heat of biomass
The optimum response device of solution urgently development and application.But since biomass material is higher containing potassium, water content, at the same biomass material with
And pyrolysis char and carrier difference of specific gravity it is big, at present in the world in typical fast pyrolysis process, generally existing Mass and heat transfer with
Band ash in response regulatory, oil, High water cut, liquid yield be low in oil, oil gas coking and blocking, semicoke carrier it is different return to material, bio oil adds
Hot autohemagglutination, fluidized gas dilution dry gas and energy consumption, the melting containing potassium carrier lead to the dead bed of bed material coking, biomass material drying, reaction
Device mechanical moving element high temperature wear, the safe outlet of semicoke and clean utilization etc. influence biomass fast pyrogenation skilled industry amplification
With ten a great problems of long-period stable operation.
A kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process that the present inventor proposes
(ZL200810000615.9) it is coupled for downlink from mixed fluidized bed reactor and fluid bed regenerator, forms a solid thermal and carry
The reaction regeneration coupled system of body circulation realizes Mass and heat transfer and the regulation reacted.It is separated although being classified by heat carrier, greatly
Middle particle heat carrier eliminates oil caused by heat ash by the pyrolysis of downlink pyrolysis reactor, the grey outlet of molecule heat from source
Middle band ash problem.But separation is not classified after biomass powder is dry, fine particle therein can also be grey from band in oil is generated on source
Phenomenon.Oil gas is not fractionated directly, and High water cut problem not can effectively solve in oil.In addition oil gas coking and blocking, semicoke carrier
It is different to return to material, bio oil heating autohemagglutination and the dry problem of biomass material to perplex biomass always self-mixing downflow fluidized bed quickly
The industrialization promotion of pyrolytic process.
3. summary of the invention
One kind that the object of the invention is to propose to overcome deficiency existing for existing biomass pyrolysis liquefaction technology
Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling multi-production process, both thoroughly solves biomass pyrolysis liquefaction
Band ash in Mass and heat transfer and response regulatory, oil, High water cut, liquid yield be low in oil, oil gas coking and blocking, semicoke carrier is different returns to
Material, bio oil heating autohemagglutination, fluidized gas dilution dry gas and energy consumption, the melting containing potassium carrier cause the dead bed of bed material coking, biomass former
Expect that 11 large-engineeringizations of drying, the regulation of reactor mechanical moving element high temperature wear, semicoke volatile matter and clean utilization etc. are total
Property problem, avoid the security risk of secondary pollution and the kindling of semicoke outlet, maximize and obtain liquid product, obtain compared with high fever
The combustion gas of value is for generating electricity, simple flow, reduces investment.
Technical solution of the present invention:
The purpose of the present invention is by the way that biomass powder and heat carrier are realized classification separation, big-and-middle particulate vector and biology
Matter is pyrolyzed by downlink pyrolysis reactor, biomass fine powder is sent directly into gasification riser gasification heating, and fine-grained carrier is direct
Outlet does Si-K fertilizer, melts from grey band in oil, semicoke clean utilization and biomass ash is eliminated on source using and containing potassium carrier
Lead to the problem of the dead bed of bed material coking.It is characterized in that the lower part of hot-air riser is arranged in biomass powder entrance, in hot-air
Gas-solid second-stage separator, gaseous phase outlet and the second level gas-solid separator entrance phase of level-one gas-solid separator are set at the top of riser
Even, the solid outlet of level-one gas-solid separator at the top of top feed bin and rotary table feeder and downlink pyrolysis reactor by being connected to；
The solid outlet of the direct outlet of the gaseous phase outlet of second level gas-solid separator, second level gas-solid separator passes through semicoke returning charge valve and gasification
Promote bottom of the tube connection；The riser that gasifies is that gas distributor and air inlet pipe is arranged in bottom, and inertia gas-solid separator is arranged in top；
The solid outlet of inertia gas-solid separator at the top of higher temperature carrier returning charge controller and downlink pyrolysis reactor by being connected to, synthesis gas
Outlet is communicated with the entrance of heat carrier second level gas-solid separator；The solid outlet and fine ash of heat carrier second level gas-solid separator are cooling
Feed bin, gaseous phase outlet pass through water- to-water heat exchanger and air heat exchanger and pyrolysis dry gas outlet；Downlink pyrolysis reactor bottom is set
Oil gas gas-solid separator is set, oil gas gas-solid separator bottom promotes bottom of the tube with gasification by semicoke returning charge valve and is connected to, and gas phase goes out
Mouth is connected with oil gas fractionating column；Air pressurized machine by air heat exchanger all the way with hot-air promoted bottom of the tube be connected to, all the way with
Gasification promotes the air inlet pipe connection of bottom of the tube setting；Water- to-water heat exchanger steam (vapor) outlet also promotes the air inlet pipe of bottom of the tube setting with gasification
Connection.
Desuperheating section and two sections of rectifying tower internals are arranged in oil gas fractionating column, from top to bottom the outlet of setting pyrolysis dry gas, the wooden vinegar
Liquid outlet, light oil outlet, heavy oil outlet.
The operation temperature of gasification riser is 750 DEG C -1000 DEG C.
At the top of downlink pyrolysis reactor, the high-temperature heat carrier and rotary feeding that are discharged by higher temperature carrier returning charge controller
The biomass powder volume ratio of device outflow is 2-8:1.
The outlet reaction temperature of downlink pyrolysis reactor is 450 DEG C -600 DEG C.
The outlet temperature of air heat exchanger is not more than 450 DEG C.
The present invention carrys out embodiment to describe the features of the present invention in detail.
4. Detailed description of the invention
Attached drawing 1 is the device of the invention structural schematic diagram.The drawing of attached drawing sets bright as follows:
1, gasify riser 2, gas distributor 3, air inlet pipe 4, inertia gas-solid separator 5, higher temperature carrier returning charge control
Device 6 processed, heat carrier second level gas-solid separator 7, fine ash cooling feed bin 8, downlink 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, booster fan 15, hot-air are promoted
Pipe 16, synthesis gas level-one gas-solid separator 17, top feed bin 18, rotary table feeder 19, synthesis gas second level gas-solid separator
20, air outlet slit 21, biomass powder entrance 22, pyrolysis dry gas export 23, semicoke returning charge valve 24, water- to-water heat exchanger 25, air
Heat exchanger 26, gas outlet.
The device of the invention design feature is described in detail with reference to the accompanying drawings and examples.
5. specific embodiment
Biomass powder entrance (21) setting is set at the top of hot-air riser (15) in the lower part of hot-air riser (15)
Gas-solid second-stage separator is set, the gaseous phase outlet of level-one gas-solid separator (16) is connected with second level gas-solid separator (19) entrance, and one
The solid outlet of grade gas-solid separator (16) passes through top feed bin (17) and rotary table feeder (18) and downlink pyrolysis reactor
(8) top connection；The direct outlet of gaseous phase outlet of second level gas-solid separator (19), the solid of second level gas-solid separator (19) go out
Mouth is connected to by semicoke returning charge valve (23) with gasification riser (1) bottom；Gasify riser (1) as bottom setting gas distribution
Inertia gas-solid separator (4) are arranged in device (2) and air inlet pipe (3), top；The solid outlet of inertia gas-solid separator (4) passes through height
It is connected at the top of warm carrier returning charge controller (5) and downlink pyrolysis reactor (8), syngas outlet and heat carrier second level gas solid separation
The entrance of device (6) communicates；The solid outlet and fine ash of heat carrier second level gas-solid separator (6) are cooling feed bin (7), and gaseous phase outlet is logical
Water- to-water heat exchanger (24) and air heat exchanger (25) is crossed to be connected to pyrolysis dry gas outlet (22)；Downlink pyrolysis reactor (8) bottom is set
Oil gas gas-solid separator (9) are set, oil gas gas-solid separator (9) bottom passes through semicoke returning charge valve (23) and gasification riser (1) bottom
Portion's connection, gaseous phase outlet are connected with oil gas fractionating column (10)；Air pressurized machine (14) by air heat exchanger (25) all the way with heat
The connection of air riser (15) bottom is connected to the air inlet pipe of gasification riser (1) bottom setting all the way；Water- to-water heat exchanger (24)
Steam (vapor) outlet is also connected with the air inlet pipe of gasification riser (1) bottom setting.
Desuperheating section and two sections of rectifying tower internals are arranged in oil gas fractionating column (10), from top to bottom the outlet of setting pyrolysis dry gas
(22), wood vinegar outlet (13), light oil outlet (12), heavy oil outlet (11).
The operation temperature of gasification riser (1) is 750 DEG C -1000 DEG C.
The high-temperature heat carrier being discharged at the top of downlink pyrolysis reactor (8) by higher temperature carrier returning charge controller (5) and rotation
The biomass powder volume ratio for rotating into glassware (18) outflow is 2-8:1.
The outlet reaction temperature of downlink pyrolysis reactor (8) is 450 DEG C -600 DEG C.
The outlet temperature of air heat exchanger (25) is not more than 450 DEG C.
Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling multi-joint-production apparatus provided by the present invention, pass through by
Biomass powder and heat carrier realize that classification separation, big-and-middle particulate vector and biomass pass through the pyrolysis of downlink pyrolysis reactor, life
Substance fine powder and pyrolysis char are sent directly into gasification riser gasification heating, and the thin direct outlet of heat carrier does Si-K fertilizer, from source
On solve semicoke clean utilization, eliminate band ash in oil, fluidized gas dilution dry gas and energy consumption and biomass ash are using and containing potassium
Carrier melts the problem for leading to the dead bed of bed material coking.Utilize the high gas velocity of gasification riser, the freely falling body of down pipe and half
Burnt material returning device eliminates that semicoke carrier is different to return to material problem；It is solved using two-tube (downlink reaction tube and gasification riser) coupling
Mass and heat transfer and the regulation reacted and the problem of reactor mechanical moving element high temperature wear；It is solved using oil and gas straight fractional distillation
High water cut problem in oil gas coking and blocking and bio oil heating autohemagglutination and oil；Using hot-air dried biomass, solves life
Raw material of substance dries problem, improves pyrolysis heating rate to improve liquid yield, these technical measures integrate, thus
It solves the 11 large-engineering general character problems for influencing biomass fast pyrogenation skilled industry amplification and long-period stable operation, disappears
In addition to perplexing the self-mixing downflow fluidized bed fast pyrogenation of biomass-gasification coupling multi-production process industrialization promotion bottleneck.
The liquid yield of different biomass fast pyrogenations: pine powder 68%, Poplar Powder 62%, corn stover 39%, cotton
Stalk 55%, oil in containing ash less than 0.2%, it is aqueous less than 1%；About 2100 kilocalorie of mixed gas calorific value, Si-K fertilizer yield are
10% or so.
Claims (6)
1. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device, it is characterized in that biomass powder entrance is arranged in heat
The lower part of air riser, is arranged gas-solid second-stage separator at the top of hot-air riser, and the gas phase of level-one gas-solid separator goes out
Mouthful be connected with second level gas-solid separator entrance, the solid outlet of level-one gas-solid separator pass through top feed bin and rotary table feeder and
Connection at the top of downlink pyrolysis reactor；The direct outlet of the gaseous phase outlet of second level gas-solid separator, the solid of second level gas-solid separator
Outlet promotes bottom of the tube with gasification by semicoke returning charge valve and is connected to；The riser that gasifies is that gas distributor and air inlet is arranged in bottom
Inertia gas-solid separator is arranged in pipe, top；The solid outlet of inertia gas-solid separator is by higher temperature carrier returning charge controller under
Connection, syngas outlet are communicated with the entrance of heat carrier second level gas-solid separator at the top of row pyrolysis reactor；Heat carrier second level gas
The cooling feed bin of the solid outlet and fine ash of solid separator, gaseous phase outlet are gone out by water- to-water heat exchanger and air heat exchanger with pyrolysis dry gas
Mouth connection；Oil gas gas-solid separator is arranged in downlink pyrolysis reactor bottom, and oil gas gas-solid separator bottom passes through semicoke returning charge valve
It promotes bottom of the tube with gasification to be connected to, gaseous phase outlet is connected with oil gas fractionating column；Air pressurized machine by air heat exchanger all the way with
Hot-air promotes bottom of the tube connection, and the air inlet pipe for promoting bottom of the tube setting with gasification all the way is connected to；Water- to-water heat exchanger steam (vapor) outlet
The air inlet pipe for promoting bottom of the tube setting with gasification is connected to.
2. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device according to claim 1, it is characterised in that
The operation temperature of gasification riser is 750 DEG C -1000 DEG C.
3. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device according to claim 1, it is characterised in that
At the top of downlink pyrolysis reactor, what the high-temperature heat carrier and rotary table feeder being discharged by higher temperature carrier returning charge controller flowed out
Biomass powder volume ratio is 2-8:1.
4. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device according to claim 1, it is characterised in that
It is 450 DEG C -600 DEG C that downlink pyrolysis reactor, which exports reaction temperature,.
5. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device according to claim 1, it is characterised in that
The outlet temperature of air heat exchanger is not more than 450 DEG C.
6. biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device according to claim 1, it is characterised in that
Desuperheating section and two sections of rectifying tower internals are arranged in oil gas fractionating column, and the outlet of setting pyrolysis dry gas, wood vinegar export, are light from top to bottom
Oil export, heavy oil outlet.
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| CN201811501372.7A CN109628155A (en) | 2018-12-10 | 2018-12-10 | Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device |
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| CN201811501372.7A CN109628155A (en) | 2018-12-10 | 2018-12-10 | Biomass downlink cycle bed millisecond pyrolysis liquefaction-gasification coupling device |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102191088A (en) * | 2011-04-12 | 2011-09-21 | 浙江大学 | Solid fuel double fluidized bed thermal pyrolysis grade transformation device and method |
| US20130019529A1 (en) * | 2010-03-23 | 2013-01-24 | Wuhan Kaidi Engineering Technology Research Institute Co., Ltd. | Method and system for producing synthesis gas |
| CN106190214A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
-
2018
- 2018-12-10 CN CN201811501372.7A patent/CN109628155A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130019529A1 (en) * | 2010-03-23 | 2013-01-24 | Wuhan Kaidi Engineering Technology Research Institute Co., Ltd. | Method and system for producing synthesis gas |
| CN102191088A (en) * | 2011-04-12 | 2011-09-21 | 浙江大学 | Solid fuel double fluidized bed thermal pyrolysis grade transformation device and method |
| CN106190214A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Biomass downlink cycle bed millisecond pyrolysis liquefaction device |
| CN107502388A (en) * | 2017-09-11 | 2017-12-22 | 哈尔滨工业大学 | Two sections of low temperature gasification device and methods based on low order fuel autocatalysis |
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