CN105925289A - Apparatus for preparing low-tar fuel gas through combining gasification and dry distillation - Google Patents
Apparatus for preparing low-tar fuel gas through combining gasification and dry distillation Download PDFInfo
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- CN105925289A CN105925289A CN201610550772.1A CN201610550772A CN105925289A CN 105925289 A CN105925289 A CN 105925289A CN 201610550772 A CN201610550772 A CN 201610550772A CN 105925289 A CN105925289 A CN 105925289A
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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
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
-
- 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
- C10J3/80—Other features with arrangements for preheating the blast or the water vapour
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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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
- 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
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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
- 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
- C10J2300/095—Exhaust gas from an external process for purification
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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
- 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
- C10J2300/0959—Oxygen
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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
- 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
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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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
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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- 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
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- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Industrial Gases (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention relates to an apparatus for preparing low-tar fuel gas through combining gasification and dry distillation. The apparatus comprises a fluidized bed gasification furnace (3), a cyclone separator (4), a slag collecting device (5), a gasifying agent supply system, microwave heating devices (12), second plasma torches (17), a fluidized bed dry distillation furnace (2-1), a built-in gas-solid separator (2-2), a syngas and coal gas processor (2-3) and first plasma torches (2-11). The apparatus is suitable for preparing coal gas through catalytic conversion and non-catalytic conversion of coal, and has the advantages of high thermal efficiency, easy large-scale formation, long-term stable running, high coal conversion rate, low coke and dust content of fuel gas, and efficient sensible heat recovery of the syngas.
Description
Technical field
The present invention relates to coal chemical technology application, prepare low tar particularly to a kind of combined vaporizing dry distilling
Gas combustion apparatus.
Background technology
Coal Chemical Industry, with coal as raw material, is prepared solid fuel through Physical Processing, is made coal be converted into gas through chemical process
Fluid fuel, liquid fuel, coke and chemicals, include coal gasification, liquefaction, coking etc. and utilize route.
Pyrolysis of coal is coal process change, and pilot process as particularly important in techniques such as gasification, liquefaction, coking, at anoxybiotic
Or partial gasification and the liquefaction of coal under anoxia condition, can be realized, prepare coal gas and tar.
Coal gasification is broadly divided into fixed bed gasification, fluidized gasification and entrained flow gasification.Fluidized bed coal gasification skill
Art is because of the Main way that it is extensive, efficient, coal adaptability becomes by force gasification technology development, fluidized gasification
The Exposure degree of stove high-temperature synthesis gas is one of difficult problem of gasification technology, goes out gasification furnace high-temperature nuclei temperature and exists
More than 1000 DEG C, synthesis gas high temperature Exposure degree mode mainly has waste heat boiler, water Quench and chemical heat to reclaim.
Chemical heat reclaims the sensible heat that can be reclaimed one section of high-temperature synthesis gas of giving vent to anger stove by the pyrolysis absorption energy of coal.Stream
Changing bed gasification furnace and can use dry ash extraction and slag tap two ways, dry ash extraction efficiency of carbon con version is relatively low, required
Dreg removing system and running cost are high；Slag tap can reduce carbon content in lime-ash, but required energy consumption is high, system thermal
Energy utilization ratio is low.Applicant is through comprehensively retrieval and in-depth study, and prior art not yet provides a kind of easy
Produce in maximizing, stable, coal conversion is high, synthesis gas Exposure degree efficiently, system thermal usefulness high,
Combustion gas contains the Coal Gasification dry distilling co-generation system and method that Jiao is low, dust is few.
Summary of the invention
In order to overcome, coal thermal transition efficiency in prior art is low, combustion gas is high containing burnt dustiness, combustion gas sensible heat profit
With unreasonable, system thermal usefulness is low, equipment is prone to slagging scorification, cannot be applicable to the catalysis of coal by same set of system
Convert and on-catalytic converts the technical problem preparing combustion gas, it is necessary to design the coal gas that can solve the problems referred to above
Change dry distilling combined production device and method.
A kind of combined vaporizing dry distilling provided of the present invention prepares low tar gas combustion apparatus, including coal gasification system
System (1) and dry distillation of coal system (2).Wherein, described gasification system (1) including: fluidized-bed gasification furnace (3),
Cyclone separator (4), slag collection device (5) and gasifying agent supply system；Described fluidized-bed gasification furnace (3)
Including body of heater (6) and shell (10), body of heater (6) interior bottom arranges conical distribution plate (7), conical distribution plate
(7) the coal charge entrance (8) being provided above and the burnt entrance (9) of ash；Described gasification furnace (3) top arranges and passes through
Wear the syngas outlet (11) of described body of heater (6) and shell (10), burner hearth (6) and shell (10) to be formed
Toroidal cavity, microwave heating equipment (12), described microwave heating equipment (12) are set in described toroidal cavity
It is arranged between conical distribution plate (7) and syngas outlet (11)；Conical distribution plate (7) the middle part row of offering
Cinder notch (13), slag-drip opening (13) is connected with slag collection device (5) by scum pipe (14)；Taper divides
Forming air chamber (15) between fabric swatch (7) lower section and shell (10) low head, gasifying agent air inlet pipe (16) is passed through
Wear described shell (10) and body of heater (6) is arranged.Described dry distillation of coal system (2) include fluidized bed dry distillation stove (2-1),
Gas-solid separator (2-2) and synthesis gas coal gas processor (2-3)；Described fluidized bed dry distillation stove (2-1) includes
One body of heater (2-4), the first body of heater (2-4) interior bottom arrange the first conical distribution plate (2-5), the first taper divides
The first coal charge entrance (2-6) that fabric swatch (2-5) is provided above；First conical distribution plate (2-5) the middle part row of offering
Jiao Kou (2-7), coke discharging mouth (2-7) is connected by the first coke discharging tube (2-8) entrance (9) burnt with described ash；
Fluidizing gas distributing chamber (2-9) is formed between first conical distribution plate (2-5) lower section and the first body of heater (2-4) inwall；
Run through the fluidizing gas that on the first body of heater (2-4) outer wall, setting connects with described fluidizing gas distributing chamber (2-9) to enter
Airduct (2-10)；Described gas-solid separator (2-2) is built in the top of described fluidized bed dry distillation stove (2-1),
Described gas-solid separator (2-2) gas outlet is connected with synthesis gas coal gas processor (2-3) air inlet by pipeline；
Synthesis gas coal gas reason device (2-3) top arranges multiple first plasmatorch (2-11), synthesis gas coal gas processor (2-3)
Gas outlet is sequentially connected with boiler (2-12) and gas buffer-stored tank (2-13) by the first gas pipeline.Institute
State cyclone separator (4) air inlet and gas outlet respectively with described syngas outlet pipeline (11) and described fluidisation
Gas blast pipe (2-10) connects；Described cyclone separator (4) solids discharge mouth entrance (9) burnt with described ash.
Preferably, described gas-solid separator (2-2) includes be interconnected centrifugal deduster and filter element.More
Preferably, filter element (2-13) is ceramic porous material or ferrum aluminum metal sintered porous material.
Preferably, the scum pipe (14) of described fluidized-bed gasification furnace (3) is additionally provided with two symmetrical
Second plasmatorch (17), and the second plasmatorch (17) becomes 30-60 degree angle to open with scum pipe (14) axis
Mouth is arranged obliquely.It is highly preferred that the second plasmatorch (17) becomes 45 degree with described scum pipe (14) axis
Angle opening is arranged obliquely.
Preferably, described synthesis gas coal gas reason device (2-3) is provided above multiple first plasmatorch (2-11)
Quantity be that 3-5 props up, and become circumference be arranged symmetrically with.It is highly preferred that the number of described first plasmatorch (2-11)
Amount is 4, and described first plasmatorch (2-11) manages device (2-3) vertical direction axle with described synthesis gas coal gas
Line becomes 45 degree of angle openings to arrange obliquely.
Preferably, the quantity of the gasifying agent air inlet pipe (16) of described fluidized-bed gasification furnace (3) is 4-10 root
And be even number, described many gasifying agent air inlet pipe (16) become circumference symmetrical, described gasifying agent air inlet pipe (16)
For barrel forms, central inner pipe is for by oxygen-containing gas, and the annular space between inner tube and outer tube is passed through the most oxygenous
Water vapour or reducibility gas such as dry distilling combustion gas.Set it is highly preferred that run through described conical distribution plate (7)
Putting 2-5 nozzle (19), described nozzle (19) is positioned on same circumference and is uniformly arranged.Described nozzle (19)
Nozzle is tube-in-tube structure, and the central inner pipe of described nozzle (19) is for by oxygen-containing gas, and central inner pipe is with outer
Annular space between pipe is passed through the most oxygenous water vapour；Described nozzle (19) central inner pipe front end face and its outer tube
Distance L between front end face is 20-35mm, i.e. runs through described conical distribution plate (7) and stretches in gasification furnace furnace chamber
The central inner pipe front end face of described nozzle (19) is longer than its outer tube front end face；Described nozzle (19) is by connecting
Component such as flange is connected with described gasifying agent air inlet pipe (16) compartment of terrain.Specifically he, such as, enter when gasifying agent
When the quantity of trachea (16) is 4, the quantity of described nozzle (19) is 2, first nozzle, second
Individual nozzle is connected to first gasifying agent air inlet pipe and the 3rd gasifying agent air inlet pipe, and second gasifying agent enters
The gasifying agent described air chamber of entrance (15) that trachea and the 4th gasifying agent air inlet pipe are sent into, in described air chamber (15)
Gasifying agent entered in body of heater (6) burner hearth by aperture on described conical distribution plate (7).By that analogy.
Preferably, the quantity of the fluidizing gas blast pipe (2-10) of described fluidized bed dry distillation stove (2-1) is 4-10
Root and be even number, described fluidizing gas blast pipe (2-10) becomes circumference symmetrical.It is highly preferred that run through described
First conical distribution plate (2-5) arranges 2-5 the first jet pipe (2-14), and described first jet pipe (2-14) is positioned at
On same circumference and be uniformly arranged.Described first jet pipe (2-14) passes through connecting elements (such as flange) with described
Fluidizing gas blast pipe (2-10) compartment of terrain connects.Specifically he, such as when fluidizing gas blast pipe (2-10)
When quantity is 6, the quantity of described first jet pipe (2-14) is 3,1# the first jet pipe, 2# the first jet pipe,
3# the first jet pipe is connected to 1# fluidizing gas blast pipe, 3# fluidizing gas blast pipe and 5# fluidizing gas air intake
Pipe；The high temperature entered through 2# fluidizing gas blast pipe, 4# fluidizing gas blast pipe and 6# fluidizing gas blast pipe closes
Gas is become to enter described fluidizing gas distributing chamber (2-9), the fluidizing gas in described fluidizing gas distributing chamber (2-9)
Entered in the first body of heater (2-4) burner hearth by the aperture on described first conical distribution plate (2-5).By that analogy.
Preferably, described slag collection device (5) is tube-in-tube structure, and it can be made up of inner core and urceolus, outward
In cylinder and the toroidal cavity of inner core, the snakelike heat exchange tube of two groups of independences is set；Or by inner core, middle cylinder and urceolus group
Become, the annular space flowing steam between inner core and middle cylinder, the annular space circulation oxygen between urceolus and middle cylinder.
Gasifying agent for described fluidized-bed gasification furnace (3) flows through this slag collection device (5) and reclaims heat
Rear entrance described gasifying agent air inlet pipe (16).Preferably, described slag collection device (5) is by inner core and urceolus
Composition, tube-in-tube structure toroidal cavity in two groups of coiled pipe heat exchanger tubes are set, first group of coiled pipe heat exchanger tube is used for circulating
The isolated oxygen of air separation equipment forms the oxygen of oxidant of preheating, water source (tap water or containing Organic substance
Sewage) after second group of coiled pipe heat exchanger tube heat exchange, form superheated steam, in advance through the steam of boiler (2-12) by-product
The oxygen of heat and superheated steam respectively enter the central inner pipe of described gasifying agent air inlet pipe (16) and inner tube and outer tube
Between annular space.
Preferably, described scum pipe (14) is made up of exotic material.Preferably, described exotic material
Comprise zirconium oxide and silicon oxide.
Preferably, described scum pipe (14) is additionally provided with fine ash entrance (20), and fine ash entrance (20) is positioned at institute
State the second plasmatorch (17) top；Described fine ash entrance (20) and described second plasmatorch (17)
Vertical height is 0.15-0.3m.It is highly preferred that described second plasmatorch (17) and described slag collection device
(5) it is additionally provided with for spraying on the scum pipe (14) of (close second plasmatorch (17)) at the 1/3 of spacing
Two jet pipes (18) of water vapour.It is highly preferred that described two jet pipes (18) are the most symmetrical and open
Mouth is arranged with the horizontal 40 degree of angles downwards.It is highly preferred that described second plasmatorch (17) and described slag
Scum pipe (14) long 1m between collection device (5).
Preferably, the cyclone separator (4) of described gasification system (1) include the first cyclone separator and
Second cyclone separator, described syngas outlet (11), the first cyclone separator, the second cyclone separator are successively
Connecting, the air inlet of the second cyclone separator and gas outlet are dry with the gas outlet of the first cyclone separator and coal respectively
Evaporate described fluidizing gas blast pipe (2-10) connection in system (2)；Described first cyclone separator solid goes out
Material mouth with described ash Jiao entrance (9) connect, described second cyclone separator solid fine ash discharging opening be arranged on institute
Stating fine ash entrance (19) connection on scum pipe (14), described fine ash entrance (19) is positioned at described second etc.
Ion torch (17) top；Described fine ash entrance (19) and the vertical height of described second plasmatorch (17)
For 0.15-0.3m.
A kind of method that low tar combustion gas is prepared in combined vaporizing dry distilling, described method includes: (a), be mixed with catalysis
Agent or be not mixed with the coal dust of catalyst and send into described gasification furnace through the coal charge entrance (8) of fluidized-bed gasification furnace (3)
(3) burner hearth, the gasifying agent of preheating is sent into described through the conical distribution plate (7) of described fluidized-bed gasification furnace (3)
Gasification furnace (3) burner hearth fluidizes the heat needed for described coal dust, coal dust gasification by the body of heater being positioned at gasification furnace (3)
(6) microwave heating equipment (12) and in shell (10) toroidal cavity provides, fluidized-bed gasification furnace (3)
The high-temperature synthesis gas of interior formation is drawn by the syngas outlet (11) on described gasification furnace (3)；(b), institute
State high-temperature synthesis gas fluidizing gas blast pipe through fluidized bed dry distillation stove (2-1) after cyclone separator (4) processes
(2-10) and the first conical distribution plate (2-5) enters described fluidized bed dry distillation stove (2-1) burner hearth and is used for serving as stream
Change medium and heat carrier makes by being positioned at the first coal charge entrance that described first conical distribution plate (2-5) is provided above
(2-6) enter the powder fluidized in described fluidized bed dry distillation stove (2-1) burner hearth, dry distilling forms combustion gas, described combustion
Gas is sent at synthesis gas coal gas after gas-solid separator (2-2) dedusting that fluidized bed dry distillation stove (2-1) furnace roof is built-in
Reason device (2-3)；C the first plasmatorch (2-11) that (), synthesis gas coal gas processor (2-3) top are arranged leads to
The plasma crossing arc discharge output more than 2500 DEG C makes the cracking of the tar in combustion gas, heavy hydrocarbon form little molecule
Fuel gas, the combustion gas after synthesis bottle coal treatment apparatus (2-3) processes is divided at least two parts, and a part is drawn
Entering described fluidized-bed gasification furnace (3) coal charge in fluidized furnace, another part reclaims heat through boiler (2-12)
Gas buffer storage tank (2-13) is sent into after byproduct steam.
Preferably, above-mentioned combined vaporizing dry distilling is prepared the method for low tar combustion gas and is used the above-mentioned associating of the present invention
Gasification dry distilling is prepared low tar gas combustion apparatus and is implemented.
Preferably, the gasifying agent of above-mentioned preheating comprise oxygen and steam, described oxygen is separated by air separation plant
Preparing, described steam is superheated steam.It is highly preferred that described superheated steam includes that water source adds through boiler (2-12)
Hot byproduct steam is again through the interlayer of jacket type structure of described fluidized-bed gasification furnace (3) slag collection device (5)
The superheated steam that cavity is formed after reclaiming heat, described water source includes tap water and/or containing organic sewage.
Preferably, gasification temperature is 700-850 DEG C, and vapor pressure is 0.1-0.4MPa.It is highly preferred that gasification temperature is
780-820 DEG C, vapor pressure is 0.25-0.35MPa.Preferably, in gasification furnace, the mass ratio of steam and coal is
0.3-0.8:1, oxygen is 0.3-0.6:1 with the mass ratio of coal.It is highly preferred that the mass ratio of steam and coal in gasification furnace
For 0.5-0.7:1, oxygen is 0.4-0.5:1 with the mass ratio of coal.
Preferably, the cyclone separator (4) of described gasification system (1) include the first cyclone separator and
Second cyclone separator, solid particle that the first cyclone separator separates and through fluidized bed dry distillation stove (2-1) the
The semicoke that one coke discharging tube (2-8) is discharged is recycled into by the burnt entrance (9) of the ash on fluidized-bed gasification furnace (3)
Fluidized-bed gasification furnace (3)；It is thin that the second isolated fine ash of cyclone separator is sent on described scum pipe (14)
Ash entrance (20), be positioned at described fine ash entrance (20) lower section the second plasmatorch (17) output 3000 DEG C with
Upper flame of centre, makes fine ash and through fluidized-bed gasification furnace (3) described conical distribution plate (7) slag-drip opening (13)
The ash melting discharged, two jet pipes (18) being provided with on described scum pipe (14) spray into water vapor acting
Lower gasification further forms synthesis gas.
Compared with prior art coal reforming unit, the present invention has the advantage that
(1), apparatus of the present invention can realize coal gasification, dry distilling coproduction, the fluidized gasification of employing independent operating
Stove and fluidized bed pyrolysis stove implement gasification and retorting operation respectively, are easily controlled and are suitable for production of maximizing.
(2), gasification furnace use microwave heating, make coal to heat the most simultaneously, the efficiency of heating surface
High, improve gasification reaction, be accurately controlled gasification reaction temperature, especially the catalysis gas to coal by microwave heating
Change reaction effect to become apparent from；The device that invention provides can be simultaneously suitable for coal catalytic gasification dry distilling coproduction and coal
Non-catalyzed gasification dry distilling coproduction.
(3), apparatus of the present invention using high-temperature gasification synthesis gas as the fluidizing agent of fluidized bed dry distillation stove and heat
Carrier, makes full use of the heat energy in system to increase the production of combustion gas, avoids using the cooling of water Quench to cause simultaneously
Energy loss and formed contaminated wastewater；Decrease the investment and maintenance cost using boiler recovery heat to bring.
(4), the built-in gas-solid separator of fluidized bed pyrolysis stove includes be interconnected centrifugal deduster and filter element
The combustion gas dustiness of self-fluidized type bed pyrolysis oven can be used less than 8mg/Nm3, by built-in for above-mentioned gas-solid separator fluidisation
Bed pyrolysis oven can significantly decrease tar and result in blockage in the accumulation of filter element surface, extends filter element and uses
Life-span, owing in fluidized bed dry distillation stove, top temperature is kept above 550 DEG C, the tar in combustion gas hardly with fine ash
Cohesion.
(5), the synthesis gas coal gas processor of the first plasmatorch being provided with by top is to through dedusting combustion gas
Thermal cracking, the plasma of the first plasmatorch arc discharge output more than 2500 DEG C makes the tar in combustion gas, weight
The matter hydrocarbon pyrolysis forms little molecule fuel gas, adds fuel gases calorific value, and after treated thermal cracking, combustion gas is coal-tar middle oil contains
Amount, less than 5ppm, can be directly used for electromotor or electromotor combustion power generation.
(6), boiler byproduct steam is set as fluidized-bed gasification furnace gasifying agent after synthesis gas coal gas processor,
Achieve thermal effect to utilize；Using the Partial cleansing combustion gas after recovered heat as fluidized-bed gasification furnace fluidizing agent,
Reduce the input of fluidized bed medium, add combustion gas active component concentration and improve fuel gases calorific value.
(7), the cyclone separator of fluidized-bed gasification furnace comprises the first cyclone separator and second whirlwind of series connection
Separator is used for degree of depth separating high-temp synthesis gas entrained solid granule, reduces the built-in gas-solid of fluidized bed dry distillation stove
Separate operating pressure；Jiao that the coarse granule separated by first cyclone separator and fluidized bed dry distillation fire grate Jiao Kou discharge
Fluidized-bed gasification furnace gasification is sent in charcoal circulation, improves charcoal percent conversion.Arrange on fluidized-bed gasification furnace scum pipe
The second plasmatorch that many symmetrical openings are arranged obliquely can produce more than 3000 DEG C flame of centre, and
The fine ash entrance that the two isolated fine ash of cyclone separator are sent on fluidized-bed gasification furnace scum pipe is discharged with slag-drip opening
Slag mixing, melted under 3000 DEG C of conditions above, the jet pipe being provided with by scum pipe is sprayed into steam and both filled
Synthesis gas is formed with the gasification of melted carbon material when slag cooling is served as again gasifying agent by coolant.
(8), run through the nozzle that tube-in-tube structure is set on fluidized-bed gasification furnace distribution grid, enhance coal in burner hearth
Powder and the mixed effect of gasifying agent, it is to avoid distribution grid near zone forms dead band, cause sintering to damage distribution grid.
Run through on fluidized bed dry distillation stove distribution grid and jet pipe is set, enhance coal dust and the turbulent closure scheme effect of heat carrier in burner hearth
Really, homogeneous heating, reduces the formation of tar.
Accompanying drawing explanation
Fig. 1 is that low tar gas combustion apparatus schematic diagram is prepared in the combined vaporizing dry distilling of the present invention.
In figure, 1, gasification system；2, dry distillation of coal system；3, fluidized-bed gasification furnace；4, cyclonic separation
Device；5, slag collection device；6, body of heater；7, conical distribution plate；8, coal charge entrance；9, the burnt entrance of ash；
10, shell；11, syngas outlet；12, microwave heating equipment；13, slag-drip opening；14, scum pipe；15、
Air chamber；16, gasifying agent air inlet pipe；17, the second plasmatorch；18, jet pipe；19, nozzle；20, fine ash
Entrance；2-1, fluidized bed dry distillation stove；2-2, gas-solid separator；2-3, synthesis gas coal gas processor；2-4,
One body of heater；2-5 the first conical distribution plate；2-6, the first coal charge entrance；2-7, coke discharging mouth；2-8, the first coke discharging
Pipe；2-9, fluidizing gas distributing chamber；2-10, fluidizing gas blast pipe；2-11, the first plasmatorch；2-12、
Boiler；2-13, gas buffer storage tank；2-14, the first jet pipe.
Detailed description of the invention
Below by embodiment, and combine accompanying drawing, technical scheme is described in further detail.
Embodiment 1: after feed coal (brown coal, anthracite or jet coal) drying processes, water content is 6-10wt%,
Feed coal after dehydration is size-reduced, sieving separating goes out broken coal A and 4-10mm being less than 16mm more than 10mm
Broken coal B, broken coal B and catalyst be mixed to form Mixture Density Networks C, wherein, catalyst is alkali metal or alkaline earth gold
Metal catalyst, broken coal B is 80-200:1 with the mass ratio of catalyst, and Mixture Density Networks C passes through fluidized-bed gasification furnace 3
Coal charge entrance 8 send in fluidized-bed gasification furnace, preheated gasifying agent (oxygen and steam) enters through gasifying agent
Trachea 16 is by the hole on the conical distribution plate 7 below coal charge entrance 8 in stove and runs through described conical distribution plate
The nozzle 19 of 7 is sent into fluidized-bed gasification furnace 3 burner hearth and is fluidized described Mixture Density Networks C, wherein, controls steam and coal
Mass ratio is 0.3-0.8:1, and oxygen is 0.3-0.6:1 with the mass ratio of coal, the power of regulation microwave heating equipment 12
Temperature in control gasification furnace 3 is at 700-850 DEG C, and control furnace pressure is 0.1-0.4MPa, wherein, in gasification
The top of furnace body 6, middle part and bottom respectively set thermocouple, and the high-temperature synthesis gas that in gasification furnace 3, gasification is formed is led to
Cross syngas outlet 11 and draw described body of heater 6, after cyclone separator 4 dedusting, send into fluid bed by pipeline do
The fluidizing gas blast pipe 2-10 of furnace 2-1, wherein, cyclone separator 4 includes that the first whirlwind being connected in series divides
From device and the second cyclone separator；High-temperature synthesis gas is through the first conical distribution plate of described fluidized bed dry distillation stove 2-1
2-5 and run through the jet pipe (2-14) of described first conical distribution plate 2-5 and be used for fluidizing, heating to enter through the first coal charge
Mouth 2-6 sends into broken coal A, and the combustion gas that dry distilling produces is through being built in the gas-solid at the top of described fluidized bed dry distillation stove 2-1
After separator 2-2 purifies, send into synthesis by the pipeline being connected with the outlet of described gas-solid separator 2-2 top gas
Bottle coal treatment apparatus 2-3；Wherein, described gas-solid separator 2-2 include the centrifugal deduster 2-12 that is interconnected and
Multiple first plasmatorch 2-11 electric discharges that filter element 2-13, synthesis gas coal gas processor 2-3 top is arranged are produced
Go out the plasma higher than 2500 DEG C and the tar in combustion gas, heavy hydrocarbon cracking are formed little molecule fuel gas, warp
Combustion gas after synthesis gas coal gas processor 2-3 processes is divided at least two parts, and a part of combustion gas is delivered to not through pipeline
With the described nozzle 19 gasifying agent air inlet pipe 16 (the preferably gasifying agent air inlet pipe of sleeve structure by Flange joint
Outer tube in 16) enter gasification furnace 3 air chamber 15, this Some gases hole on described conical distribution plate 7
Solid material in fluidizing burner hearth；Gas is sent in a part of combustion gas after boiler (2-12) heat exchange byproduct steam
Body buffer-stored tank (2-13).Wherein, the semicoke formed in fluidized bed dry distillation stove 2-1 is through the first conical distribution plate
The first coke discharging tube 2-8 that the coke discharging mouth 2-7 offered in the middle part of 2-5 and described coke discharging mouth 2-7 connects sends into described fluidisation
The burnt entrance 9 of ash on bed gasification furnace 3；Wherein, the burnt entrance 9 of described ash is opposite to below described coal charge entrance 8；
The first isolated coarse granule of cyclone separator in cyclone separator 4 sends into gasification furnace 3 through the burnt entrance 9 of described ash
Interior cycle gasification；The second isolated fine ash of cyclone separator is then sent on the scum pipe 14 of fluidized-bed gasification furnace 3
The fine ash entrance 19 arranged, the lime-ash that fluidized-bed gasification furnace 3 gasification produces is offered by the middle part of conical distribution plate 7
Slag-drip opening 13 enter described scum pipe 14, described lime-ash and fine ash are under gravity through fine ash entrance 19
Multiple second plasmatorch 17 that lower section is arranged form high-temperature area and add heat fusing, wherein, and described second plasma
More than 3000 DEG C flame of centre of torch 17 output, through a steam of boiler (2-12) by-product through described scum pipe 14
On below described second plasmatorch 17 arrange jet pipe 18 spray into scum pipe 14, under thermodynamic activity, warp
The steam of jet pipe 18 injection becomes V-type move, the steaming flowed up in melted lime-ash and fine ash and scum pipe 14
Vapour further gasification reaction formation synthesis gas is in scum pipe 14 enters fluidized-bed gasification furnace 3, in scum pipe 14
Slag entrance slag collection device 5 through just cooling；Wherein, described slag collection device 5 is tube-in-tube structure, its
Can be made up of inner core and urceolus, the snakelike heat exchange tube of two groups of independences is set in the toroidal cavity of urceolus and inner core；Or
Person is made up of inner core, middle cylinder and urceolus, and the annular space flowing steam between inner core and middle cylinder, between urceolus and middle cylinder
Annular space circulation oxygen；Through the O that air-separating plant obtains2And another steam of boiler (2-12) by-product divides
With high temperature furnace slag heat exchange, the O after heating during the gas access on slag collection device 5 does not enters heat exchange component2
It is respectively fed to described nozzle 19 by the inner tube of the gasifying agent air inlet pipe 16 of Flange joint and outward with superheated steam
Pipe.After testing, in slag collection device 5, carbon content is less than 4wt%, at synthesis gas coal gas processor 2-3
The combustion gas tar content of reason is more than 1500ppm, and in gas buffer storage tank (2-13), combustion gas tar content is less than
5ppm, solid particle dustiness is less than 8mg/Nm3, coal treating capacity is more than 180 tons/d, and system thermal efficiency is more than
80%, continuously-running causes system shutdown without tar blocking filter element in 2 years.
Embodiment 2: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is identical, and difference is: broken coal B directly passes through the coal of fluidized-bed gasification furnace 3
Material entrance 8 carries out non-catalyzed gasification in sending into fluidized-bed gasification furnace, and gasification temperature controls as at 830-1150 DEG C.
After testing, in slag collection device 5, carbon content is less than 3.85wt%, without synthesis gas coal gas processor 2-3 process
Combustion gas tar content more than 1378ppm, in gas buffer storage tank (2-13), combustion gas tar content is less than
4.8ppm, solid particle dustiness is less than 7.8mg/Nm3, coal treating capacity is more than 180 tons/d, and system thermal efficiency is big
In 82%, run 2 years continuously without causing system shutdown because of tar blocking filter element.
Embodiment 3: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: by described gas-solid separator built-in for fluidized bed dry distillation stove
2-2 is external, is i.e. connected to fluidized bed dry distillation stove furnace top gas by pipeline and exports, connects the long 0.3-0.6m of pipeline；
Other technological parameter is same as in Example 1, and system is run continuously 13 months and because the blocking of filter element tar causes is
System stops.
Embodiment 4: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: the described gas-solid separator 2-2 that fluidized bed dry distillation stove is built-in
Being the centrifugal deduster of two series connection, other technological parameter is same as in Example 1.After testing, slag collection dress
Put carbon content in 5 to be more than less than 4wt%, the combustion gas tar content processed without synthesis gas coal gas processor 2-3
1760ppm, in gas buffer storage tank (2-13), combustion gas tar content is less than 6.5ppm, solid particle dustiness
More than 169mg/Nm3, coal treating capacity is more than 180 tons/d, and system thermal efficiency is more than 80%, continuously-running 2
Year causes system shutdown without tar blocking filter element.
Embodiment 5: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: the described gas-solid separator 2-2 that fluidized bed dry distillation stove is built-in
Being the filter elements of two series connection, other technological parameter is same as in Example 1.System run continuously 6 months because of
Filter element blocking causes system shutdown.
Embodiment 6: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: the fine ash that the second cyclone separator is separated again by
The burnt entrance 9 of ash sends into fluidized-bed gasification furnace, and other technological parameter is same as in Example 1.After testing, system thermal
Efficiency is less than 74%, and system is run 11 months and caused system shutdown because filter element blocks；Slag collection device 5
Middle carbon content is less than 4wt%, and the combustion gas tar content processed without synthesis gas coal gas processor 2-3 is more than
1500ppm, in gas buffer storage tank (2-13), combustion gas tar content is less than 5ppm, solid particle dustiness
Less than 8mg/Nm3, coal treating capacity is more than 180 tons/d, and system thermal efficiency is less than 74%, continuously-running 2 years
System shutdown is caused without tar blocking filter element.
Embodiment 7: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: be not provided with on fluidized-bed gasification furnace scum pipe the second grade from
Sub-torch, sends into fluidized-bed gasification furnace by the fine ash of the second cyclone separator separation by the burnt entrance 9 of ash, other work
Skill parameter is same as in Example 1.After testing, in slag collection device 5, carbon content is more than 10wt%, and carbon utilizes
Rate is low.
Embodiment 8: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: does not set on fluidized-bed gasification furnace conical distribution plate 7 and runs through
The nozzle 19 of described conical distribution plate, i.e. preheating after gasifying agent (oxygen and superheated steam) and be used for serving as stream
The part circulating gas changing medium passes through the gasifying agent air inlet pipe 16 hole entrance gas on described conical distribution plate 7
Changing stove burner hearth, other technological parameter is same as in Example 1.After testing, in slag collection device 5, carbon content is little
In 4.5wt%, it is serious that system runs 14 months fluidized-bed gasification furnace conical distribution slag that hardens, and causes system to be forced to stop
Car.
Embodiment 9: this embodiment carries out combined vaporizing dry distilling and prepares method and embodiment 1 institute of low tar combustion gas
The device of the method selection carried out is different, and difference is: fluidized-bed gasification furnace slag collection device 5 is non-sleeve
Structure, i.e. gasifying agent reclaim heat without slag collection device 5 heat exchange and are sent directly into gasifying agent air inlet pipe 16, its
Its technological parameter is same as in Example 1.After testing, system thermal efficiency is less than 50%, in slag collection device 5
Carbon content is less than 4.1wt%, and the combustion gas tar content processed without synthesis gas coal gas processor 2-3 is more than
1700ppm, in gas buffer storage tank (2-13), combustion gas tar content is less than 5.3ppm, solid particle dustiness
Less than 10mg/Nm3, coal treating capacity is more than 180 tons/d, and continuously-running is made for 2 years without tar blocking filter element
Become system shutdown.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for this area
Technical staff for, the present invention can have various modifications and variations.All within the spirit and principles in the present invention,
Any modification, equivalent substitution and improvement etc. made, within being all contained in protection scope of the present invention.
Claims (10)
1. a low tar gas combustion apparatus is prepared in combined vaporizing dry distilling, including gasification system (1) and dry distillation of coal system
(2), it is characterised in that: described gasification system (1) including: fluidized-bed gasification furnace (3), cyclone separator (4),
Slag collection device (5) and gasifying agent supply system；Described fluidized-bed gasification furnace (3) include body of heater (6) and
Shell (10), the conical distribution plate (7) of body of heater (6) interior bottom setting, described conical distribution plate (7) top
The coal charge entrance (8) arranged and the burnt entrance (9) of ash；Described fluidized-bed gasification furnace (3) top is arranged to be run through
The syngas outlet (11) of described body of heater (6) and shell (10), body of heater (6) and shell (10) are formed
Arranging microwave heating equipment (12) in toroidal cavity, described microwave heating equipment (12) is arranged on conical distribution plate
(7) and between syngas outlet (11)；Slag-drip opening (13), slag-drip opening are offered in conical distribution plate (7) middle part
(13) connected with slag collection device (5) by scum pipe (14)；Described conical distribution plate (7) lower section
And forming air chamber (15) between shell (10) low head, gasifying agent air inlet pipe (16) runs through described shell (10)
Arrange with body of heater (6)；
Described dry distillation of coal system (2) includes fluidized bed dry distillation stove (2-1), gas-solid separator (2-2) and synthesis gas coal gas
Processor (2-3)；Described fluidized bed dry distillation stove (2-1) includes the first body of heater (2-4), described first body of heater (2-4)
Interior bottom arranges the first conical distribution plate (2-5), described first conical distribution plate (2-5) be provided above first
Coal charge entrance (2-6)；Coke discharging mouth (2-7), described coke discharging mouth (2-7) are offered in first conical distribution plate (2-5) middle part
Connected by the first coke discharging tube (2-8) entrance (9) burnt with described ash；First conical distribution plate (2-5) lower section
And form fluidizing gas distributing chamber (2-9) between the first body of heater (2-4) inwall；Run through described first body of heater (2-4)
The fluidizing gas blast pipe (2-10) connected with described fluidizing gas distributing chamber (2-9) is set on outer wall；Described gas
Solid separator (2-2) is built in described fluidized bed dry distillation stove (2-1) top, described gas-solid separator (2-2)
Gas outlet is connected with synthesis gas coal gas processor (2-3) air inlet by pipeline；Synthesis gas coal gas reason device (2-3)
Top arranges multiple first plasmatorch (2-11), and synthesis gas coal gas reason device (2-3) gas outlet of place delays with gas
Rush storage tank (2-13) connection；
Described cyclone separator (4) air inlet and gas outlet respectively with described syngas outlet (11) and described fluidized gas
Body blast pipe (2-10) connects；Described cyclone separator (4) solids discharge mouth entrance (9) burnt with described ash.
Low tar gas combustion apparatus is prepared in combined vaporizing dry distilling the most according to claim 1, it is characterised in that: described
Two symmetrical the second plasmatorch (17) it are additionally provided with on the scum pipe (14) of fluidized-bed gasification furnace (3),
And second plasmatorch (17) become 30-60 degree angle opening to arrange obliquely with scum pipe (14) axis；Preferably,
Described second plasmatorch (17) becomes 45 degree of angle openings to arrange obliquely with described scum pipe (14) axis.
Low tar gas combustion apparatus is prepared in combined vaporizing dry distilling the most according to claim 1, it is characterised in that: described
Gas-solid separator (2-2) includes centrifugal deduster and the filter element being arranged in series；Preferably, described filtering element excessively
Part is ceramic porous material or ferrum aluminum metal sintered porous material.
Low tar gas combustion apparatus is prepared in combined vaporizing dry distilling the most according to claim 3, it is characterised in that: according to
Low tar gas combustion apparatus is prepared in combined vaporizing dry distilling described in claim 1, it is characterised in that: described synthesis gas
Coal gas reason device (2-3) top arranges 3-5 and props up into the first plasmatorch (2-11) that circumference is arranged symmetrically with；Preferably,
The quantity of described first plasmatorch (2-11) is 4, described first plasmatorch (2-11) and described synthesis
Bottle coal gas reason device (2-3) vertical direction axis becomes 45 degree of angle openings to arrange obliquely.
5. prepare low tar gas combustion apparatus according to the combined vaporizing dry distilling described in claim 1-4 any one claim,
It is characterized in that: described slag collection device (5) is the tube-in-tube structure being made up of inner core, middle cylinder and urceolus, interior
Cylinder collects slag, the annular space flowing steam between inner core and middle cylinder, the annular space circulation oxygen between urceolus and middle cylinder.
Low tar gas combustion apparatus is prepared in combined vaporizing dry distilling the most according to claim 5, it is characterised in that: described
Cyclone separator (4) includes the first cyclone separator and the second cyclone separator, described syngas outlet (11),
First cyclone separator, the second cyclone separator are sequentially connected with, the air inlet of the second cyclone separator and gas outlet
Respectively with the described fluidizing gas blast pipe (2-10) in the gas outlet of the first cyclone separator and dry distillation of coal system (2)
Connection；Described first cyclone separator solids exit mouth entrance (9) burnt with described ash connects, described second whirlwind
Separator solid fine ash discharging opening connects with the fine ash entrance (19) being arranged on described scum pipe (14), institute
State fine ash entrance (19) and be positioned at described second plasmatorch (17) top.
7. prepare low tar gas combustion apparatus according to the combined vaporizing dry distilling described in claim 1-6 any one claim,
It is characterized in that: the quantity of the gasifying agent air inlet pipe (16) of described fluidized-bed gasification furnace (3) is 4 and Cheng Yuan
Week is symmetrical, and described gasifying agent air inlet pipe (16), for be made up of inner tube and the outer tube being set in outside inner tube, is passed through
Wear described conical distribution plate (7) to arrange 2 and be positioned on same circumference and symmetrically arranged nozzle (19), described
Nozzle (19) nozzle is the tube-in-tube structure being made up of with the outer tube being set in outside inner tube inner tube, described nozzle (19)
Distance L between central inner pipe front end face and its outer tube front end face is 20-35mm, and described nozzle (19) passes through method
Blue and described gasifying agent air inlet pipe (16) compartment of terrain is connected.
8. the method that low tar combustion gas is prepared in a combined vaporizing dry distilling, it is characterised in that: described method includes: (a),
It is mixed with catalyst or is not mixed with the coal dust of catalyst and sends into institute through the coal charge entrance (8) of fluidized-bed gasification furnace (3)
Stating gasification furnace (3) burner hearth, the gasifying agent of preheating is through the conical distribution plate (7) of described fluidized-bed gasification furnace (3)
Send into described gasification furnace (3) burner hearth and fluidize the heat needed for described coal dust, coal dust gasification by being positioned at gasification furnace (3)
Body of heater (6) and shell (10) toroidal cavity in microwave heating equipment (12) provide, fluidized-bed gasification furnace
(3) high-temperature synthesis gas formed in is drawn by the syngas outlet (11) on described gasification furnace (3)；(b)、
Described high-temperature synthesis gas after cyclone separator (4) processes through the fluidizing gas air intake of fluidized bed dry distillation stove (2-1)
Pipe (2-10) and the first conical distribution plate (2-5) enter described fluidized bed dry distillation stove (2-1) burner hearth and are used for serving as
Fluidizing agent and heat carrier make the first coal charge being provided above by being positioned at described first conical distribution plate (2-5) enter
Mouth (2-6) enters the powder fluidized in described fluidized bed dry distillation stove (2-1) burner hearth, dry distilling forms combustion gas, described
Synthesis gas coal gas is sent in combustion gas after gas-solid separator (2-2) dedusting that fluidized bed dry distillation stove (2-1) furnace roof is built-in
Processor (2-3)；C the first plasmatorch (2-11) that (), synthesis gas coal gas processor (2-3) top are arranged
The cracking of the tar in combustion gas, heavy hydrocarbon is made to form little point by the plasma of arc discharge output more than 2500 DEG C
Sub-fuel gas, the combustion gas after synthesis bottle coal treatment apparatus (2-3) processes is divided at least two parts, a part
Introducing described fluidized-bed gasification furnace (3) coal charge in fluidized furnace, another part reclaims heat through boiler (2-12)
Gas buffer storage tank (2-13) is sent into after amount byproduct steam.
The method that low tar combustion gas is prepared in combined vaporizing dry distilling the most according to claim 8, it is characterised in that: institute
Method of stating uses the combined vaporizing dry distilling described in claim 1-7 any one claim to prepare low tar combustion gas dress
Put enforcement.
The method that low tar combustion gas is prepared in combined vaporizing dry distilling the most according to claim 9, it is characterised in that:
Gasification temperature is 700-850 DEG C, and vapor pressure is 0.1-0.4MPa, and in gasification furnace, steam with the mass ratio of coal is
0.3-0.8:1, oxygen is 0.3-0.6:1 with the mass ratio of coal；Preferably, gasification temperature is 780-820 DEG C, gasification
Pressure is 0.25-0.35MPa, and in gasification furnace, steam is 0.5-0.7:1 with the mass ratio of coal, oxygen and the mass ratio of coal
For 0.4-0.5:1.
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| CN107227177A (en) * | 2016-09-13 | 2017-10-03 | 孔令增 | The double section gasification furnace coal gas of high temperature of semi-coke gas retort connection substitute combustion-supporting gas method for destructive distillation |
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