CN105925289B - A kind of combined vaporizing destructive distillation prepares low tar gas combustion apparatus - Google Patents
A kind of combined vaporizing destructive distillation prepares low tar gas combustion apparatus Download PDFInfo
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- CN105925289B CN105925289B CN201610550772.1A CN201610550772A CN105925289B CN 105925289 B CN105925289 B CN 105925289B CN 201610550772 A CN201610550772 A CN 201610550772A CN 105925289 B CN105925289 B CN 105925289B
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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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
-
- 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 present invention relates to a kind of combined vaporizing destructive distillation to prepare low tar gas combustion apparatus, it includes fluidized-bed gasification furnace (3), cyclone separator (4), slag collection device (5), gasifying agent supply system, microwave heating equipment (12), second plasmatorch (17), fluidized bed dry distillation furnace (2-1), built-in gas-solid separator (2-2), synthesis gas coal gas processor (2-3) and the first plasmatorch (2-11), the device can be suitably used for coal catalyzed conversion and non-catalytic conversion preparation combustion gas, thermal efficiency is high, it is easy to enlargement, longtime running is stablized, coal conversion is high, it is low that combustion gas contains burnt dustiness, synthesis gas Exposure degree is efficient.
Description
Technical field
The present invention relates to coal chemical technology application field, in particular to a kind of combined vaporizing destructive distillation prepares low tar combustion gas dress
It sets.
Background technique
Coal chemical industry prepares solid fuel using coal as raw material, through Physical Processing, make through chemical process coal be converted into gaseous fuel,
Liquid fuel, coke and chemicals include that coal gasification, liquefaction, coking etc. utilize route.Pyrolysis of coal is that coal processing turns
Change, such as gasify, liquefy, the pilot process that coking technique is particularly important, the part of coal can be achieved under anoxybiotic or anoxia condition
Gasification and liquefaction, are made coal gas and tar.
Coal gasification is broadly divided into fixed bed gasification, fluidized gasification and entrained flow gasification.In The Fluidized Bed Coal Gasification Technology is because of it
On a large scale, efficiently, coal adaptability become the Main way of gasification technology development by force, fluidized-bed gasification furnace high-temperature synthesis gas it is aobvious
Recuperation of heat is one of problem of gasification technology, and gasification furnace high-temperature synthesis gas temperature is at 1000 DEG C or more out, synthesis gas high temperature sensible heat
Way of recycling mainly has waste heat boiler, water Quench and chemical recuperation of heat.Chemical recuperation of heat can by the pyrolysis of coal absorb energy come
Recycle out the sensible heat of one section of high-temperature synthesis gas of gasification furnace.Two kinds of sides of dry ash extraction and slag tap can be used in fluidized-bed gasification furnace
Formula, dry ash extraction efficiency of carbon con version is lower, required dreg removing system and operating cost are high；Slag tap can reduce carbon content in lime-ash,
But required energy consumption is high, and system utilization efficiency of heat energy is low.Applicant is by comprehensive retrieval and in-depth study, and the prior art is not yet
There is provided one kind be easy to enlargement production, stable, coal conversion is high, synthesis gas Exposure degree efficiently, system thermal efficiency it is high,
Combustion gas is containing burnt Coal Gasification destructive distillation co-generation system and method low, dust is few.
Summary of the invention
In order to overcome coal thermal transition low efficiency, combustion gas in the prior art containing burnt dustiness, high, combustion gas sensible heat utilization does not conform to
Reason, system thermal efficiency is low, equipment is easy to slagging, can not catalyzed conversion with same set of system suitable for coal and non-catalytic conversion
The technical issues of preparing combustion gas, it is necessary to design the Coal Gasification destructive distillation combined production device and method that can solve the above problem.
Provided a kind of combined vaporizing destructive distillation of the invention prepares low tar gas combustion apparatus, including gasification system (1)
With dry distillation of coal system (2).Wherein, the gasification system (1) includes: fluidized-bed gasification furnace (3), cyclone separator (4), clinker receipts
Acquisition means (5) and gasifying agent supply system；The fluidized-bed gasification furnace (3) includes furnace body (6) and shell (10), and furnace body (6) is interior
Conical distribution plate (7) are arranged in lower part, the burnt entrance (9) of coal charge entrance (8) and ash being arranged above conical distribution plate (7)；It is described
The setting of gasification furnace (3) top runs through the syngas outlet (11) of the furnace body (6) and shell (10), burner hearth (6) and shell (10)
The toroidal cavity of formation, the toroidal cavity is interior to be arranged microwave heating equipment (12), and microwave heating equipment (12) setting exists
Between conical distribution plate (7) and syngas outlet (11)；It is opened up slag-drip opening (13) in the middle part of conical distribution plate (7), slag-drip opening (13)
It is connected to by scum pipe (14) with slag collection device (5)；It is formed between shell (10) lower head below conical distribution plate (7)
Gas chamber (15), gasifying agent air inlet pipe (16) are arranged through the shell (10) and furnace body (6).The dry distillation of coal system (2) includes
Fluidized bed dry distillation furnace (2-1), gas-solid separator (2-2) and synthesis gas coal gas processor (2-3)；Fluidized bed dry distillation furnace (the 2-
It 1) include the first furnace body (2-4), the first furnace body (2-4) interior lower part setting the first conical distribution plate (2-5), the first conical distribution plate
The first coal charge entrance (2-6) being arranged above (2-5)；Coke discharging mouth (2-7), coke discharging are opened up in the middle part of first conical distribution plate (2-5)
Mouth (2-7) is connected to by the first coke discharging tube (2-8) with the burnt entrance (9) of the ash；First conical distribution plate (2-5) lower section and first
Fluidizing gas distributing chamber (2-9) is formed between furnace body (2-4) inner wall；Setting and the stream on the first furnace body (2-4) outer wall
Change the fluidizing gas blast pipe (2-10) of gas distributing chamber (2-9) connection；The gas-solid separator (2-2) is built in the fluidisation
The top of bed gas retort (2-1), gas-solid separator (2-2) gas vent pass through pipeline and synthesis gas coal gas processor (2-
3) air inlet is connected to；Synthesis gas coal gas, which is managed, is arranged multiple first plasmatorch (2-11) at the top of device (2-3), the processing of synthesis gas coal gas
Device (2-3) gas vent is sequentially connected boiler (2-12) and gas buffer-stored tank (2-13) by the first gas pipeline.It is described
Cyclone separator (4) air inlet and air outlet respectively with the syngas outlet pipeline (11) and the fluidizing gas blast pipe
(2-10) connection；Cyclone separator (4) the solids discharge mouth and the burnt entrance (9) of the ash.
Preferably, the gas-solid separator (2-2) includes be interconnected centrifugal deduster and filter element.It is highly preferred that
Filter element (2-13) is ceramic porous material or iron aluminum metal sintered porous material.
Preferably, be additionally provided on the scum pipe (14) of the fluidized-bed gasification furnace (3) two symmetrical second it is equal from
Sub- torch (17), and the second plasmatorch (17) is arranged with scum pipe (14) axis at 30-60 degree angle opening obliquely.More preferably
Ground, the second plasmatorch (17) are arranged with the scum pipe (14) axis at 45 degree of angle openings obliquely.
Preferably, the quantity of multiple first plasmatorch (2-11) of setting is above synthesis gas coal gas reason device (2-3)
3-5 branch, and be arranged symmetrically at circumference.It is highly preferred that the quantity of first plasmatorch (2-11) be 4, described first etc.
Ion torch (2-11) is arranged with synthesis gas coal gas reason device (2-3) vertical direction axis at 45 degree of angle openings obliquely.
Preferably, the quantity of the gasifying agent air inlet pipe (16) of the fluidized-bed gasification furnace (3) is 4-10 root and is even number, institute
It is symmetrical at circumference to state more gasifying agent air inlet pipe (16), the gasifying agent air inlet pipe (16) is barrel forms, central inner pipe
For by oxygen-containing gas, it is for example dry that the annular space between inner tube and outer tube is passed through not oxygenous water vapour or reducibility gas
Evaporate combustion gas.It is highly preferred that 2-5 nozzle (19) is arranged through the conical distribution plate (7), the nozzle (19) is located at same circle
On week and it is uniformly arranged.Nozzle (19) nozzle is tube-in-tube structure, and the central inner pipe of the nozzle (19) is used for by oxygen-containing
Gas, the annular space between central inner pipe and outer tube are passed through not oxygenous water vapour；Nozzle (19) the central inner pipe front end face
Distance L is 20-35mm between its outer tube front end face, i.e., protrudes into the institute in gasification furnace furnace chamber through the conical distribution plate (7)
The central inner pipe front end face for stating nozzle (19) is longer than its outer tube front end face；The nozzle (19) by connecting elements such as flange with
Gasifying agent air inlet pipe (16) the compartment of terrain connection.Specifically he, such as when the quantity of gasifying agent air inlet pipe (16) be 4 when, institute
The quantity for stating nozzle (19) is 2, and first nozzle, second nozzle are connected to first gasifying agent air inlet pipe and third
The gasifying agent that root gasifying agent air inlet pipe, second gasifying agent air inlet pipe and the 4th gasifying agent air inlet pipe are sent into enters the gas chamber
(15), the gasifying agent in the gas chamber (15) is entered in furnace body (6) burner hearth by the aperture on the conical distribution plate (7).With
This analogizes.
Preferably, the quantity of the fluidizing gas blast pipe (2-10) of the fluidized bed dry distillation furnace (2-1) is 4-10 root and is
Even number, the fluidizing gas blast pipe (2-10) are symmetrical at circumference.It is highly preferred that running through the first conical distribution plate
2-5 the first jet pipes (2-14) are arranged in (2-5), and first jet pipe (2-14) is located on same circumference and is uniformly arranged.It is described
First jet pipe (2-14) is connect by connecting elements (such as flange) with fluidizing gas blast pipe (2-10) compartment of terrain.Specifically
He, such as when the quantity of fluidizing gas blast pipe (2-10) is 6, the quantity of first jet pipe (2-14) is 3,1# the
One jet pipe, the first jet pipe of 2#, the first jet pipe of 3# are connected to 1# fluidizing gas blast pipe, 3# fluidizing gas blast pipe and 5# stream
Change gas blast pipe；The high temperature entered through 2# fluidizing gas blast pipe, 4# fluidizing gas blast pipe and 6# fluidizing gas blast pipe
Synthesis gas enters the fluidizing gas distributing chamber (2-9), and the fluidizing gas in the fluidizing gas distributing chamber (2-9) passes through described
Aperture on first conical distribution plate (2-5) enters in the first furnace body (2-4) burner hearth.And so on.
Preferably, the slag collection device (5) is tube-in-tube structure, can be made of inner barrel and outer barrel, outer cylinder and inner cylinder
Toroidal cavity in be arranged two groups of independent snakelike heat exchange tubes；Or be made of inner cylinder, middle cylinder and outer cylinder, between inner cylinder and middle cylinder
Annular space flowing steam, annular space between outer cylinder and middle cylinder circulates oxygen.
Gasifying agent for the fluidized-bed gasification furnace (3) enters institute after flowing through the slag collection device (5) recycling heat
State gasifying agent air inlet pipe (16).Preferably, the slag collection device (5) is made of inner barrel and outer barrel, tube-in-tube structure annular
Two groups of coiled pipe heat exchanger tubes are set in cavity, and oxygen of first group of coiled pipe heat exchanger tube for ventilating air separation equipment to be isolated is formed
The oxygen of the oxidant of preheating, the steam of water source (tap water or the sewage containing organic matter) through boiler (2-12) by-product is through second group
Superheated steam is formed after the heat exchange of coiled pipe heat exchanger tube, the oxygen and superheated steam of preheating respectively enter the gasifying agent air inlet pipe (16)
Central inner pipe and inner tube and outer tube between annular space.
Preferably, the scum pipe (14) is made of heat-resisting material.Preferably, the heat-resisting material includes zirconium oxide
And silica.
Preferably, the scum pipe (14) is additionally provided with fine ash entrance (20), fine ash entrance (20) be located at described second it is equal from
Above sub- torch (17)；The vertical height of the fine ash entrance (20) and second plasmatorch (17) is 0.15-0.3m.It is more excellent
(close to the second plasmatorch at the 1/3 of selection of land, second plasmatorch (17) and the slag collection device (5) spacing
(17)) two jet pipes (18) for spraying water vapour are additionally provided on scum pipe (14).It is highly preferred that two jet pipes
(18) circumferentially symmetrical and Open Side Down and horizontal plane is arranged at 40 degree of angles.It is highly preferred that second plasmatorch
(17) scum pipe (14) long 1m between the slag collection device (5).
Preferably, the cyclone separator (4) of the gasification system (1) includes the first cyclone separator and the second whirlwind point
From device, the syngas outlet (11), the first cyclone separator, the second cyclone separator are sequentially connected, the second cyclone separator
Air inlet and gas outlet respectively with the fluidizing gas in the gas outlet of the first cyclone separator and dry distillation of coal system (2) into
Air hose (2-10) connection；The first cyclone separator solid outlet is connected to the burnt entrance (9) of the ash, second whirlwind
Separator solid fine ash discharge port is connected to the fine ash entrance (20) being arranged on the scum pipe (14), the fine ash entrance
(20) it is located above second plasmatorch (17)；The fine ash entrance (20) is vertical with second plasmatorch (17)
Height is 0.15-0.3m.
A kind of method that combined vaporizing destructive distillation prepares low tar combustion gas, which comprises (a), be mixed with catalyst or not
The coal dust for being mixed with catalyst is sent into gasification furnace (3) burner hearth, the gas of preheating through the coal charge entrance (8) of fluidized-bed gasification furnace (3)
Agent is sent into gasification furnace (3) burner hearth through the conical distribution plate (7) of the fluidized-bed gasification furnace (3) and fluidizes the coal dust, coal
Microwave heating equipment in furnace body (6) and shell (10) toroidal cavity of the heat needed for powder gasification by being located at gasification furnace (3)
(12) it provides, the high-temperature synthesis gas formed in fluidized-bed gasification furnace (3) passes through the syngas outlet (11) on the gasification furnace (3)
It draws；(b), fluidizing gas air inlet of the high-temperature synthesis gas after cyclone separator (4) processing through fluidized bed dry distillation furnace (2-1)
Pipe (2-10) and the first conical distribution plate (2-5) enter fluidized bed dry distillation furnace (2-1) burner hearth for serve as fluidizing agent and
Heat carrier makes to enter the stream by being located at the first coal charge entrance (2-6) being arranged above the first conical distribution plate (2-5)
Powder fluidized, destructive distillation in change bed gas retort (2-1) burner hearth form combustion gas, and the combustion gas is through fluidized bed dry distillation furnace (2-1) furnace roof
Synthesis gas coal gas processor (2-3) is sent into after built-in gas-solid separator (2-2) dedusting；(c), synthesis gas coal gas processor (2-
3) the first plasmatorch (2-11) that top is arranged is made in combustion gas by 2500 DEG C of arc discharge output or more of plasma
Tar, the heavy hydrocarbon pyrolysis form small molecule fuel gas, and through synthesis bottle coal treatment apparatus (2-3), treated, and combustion gas is divided at least
Two parts, a part introduce the fluidized-bed gasification furnace (3) for coal charge in fluidized furnace, and another part is recycled through boiler (2-12)
Gas buffer storage tank (2-13) is sent into after heat byproduct steam.
Preferably, the method that above-mentioned combined vaporizing destructive distillation prepares low tar combustion gas is done using the above-mentioned combined vaporizing of the present invention
It evaporates and prepares the implementation of low tar gas combustion apparatus.
Preferably, the gasifying agent of above-mentioned preheating includes oxygen and steam, and the oxygen is separated by air separation plant and is made, institute
Stating steam is superheated steam.It is highly preferred that the superheated steam includes water source through boiler (2-12) heating byproduct steam again through institute
The overheat formed after the interlayer cavity recycling heat of the jacket type structure of fluidized-bed gasification furnace (3) slag collection device (5) is stated to steam
Vapour, the water source include tap water and/or the sewage containing organic matter.Preferably, gasification temperature is 700-850 DEG C, gasification pressure
Power is 0.1-0.4MPa.It is highly preferred that gasification temperature is 780-820 DEG C, vapor pressure 0.25-0.35MPa.Preferably, gas
Changing the mass ratio of steam and coal in furnace is 0.3-0.8:1, and the mass ratio of oxygen and coal is 0.3-0.6:1.It is highly preferred that gasification furnace
The mass ratio of interior steam and coal is 0.5-0.7:1, and the mass ratio of oxygen and coal is 0.4-0.5:1.
Preferably, the cyclone separator (4) of the gasification system (1) includes the first cyclone separator and the second whirlwind point
From device, the solid particle of the first cyclone separator separation and through the first coke discharging tube of fluidized bed dry distillation furnace (2-1) (2-8) discharge
Semicoke is recycled into fluidized-bed gasification furnace (3) by the burnt entrance (9) of ash on fluidized-bed gasification furnace (3)；Second cyclone separator
The fine ash isolated is sent into the fine ash entrance (20) on the scum pipe (14), second be located at below the fine ash entrance (20)
3000 DEG C of output of plasmatorch (17) or more flame of centre, makes fine ash and through fluidized-bed gasification furnace (3) the conical distribution plate (7)
The ash melting of slag-drip opening (13) discharge, two jet pipes (18) being equipped on the scum pipe (14) spray under water vapor acting
Further gasification forms synthesis gas.
Compared with prior art coal reforming unit, of the invention is had the advantages that
(1), apparatus of the present invention are able to achieve coal gasification, destructive distillation coproduction, using independently operated fluidized-bed gasification furnace and fluidisation
Bed pyrolysis oven implements gasification and retorting operation respectively, is easy to control and is suitble to enlargement production.
(2), gasification furnace uses microwave heating, enables coal from internal to external while heating, and heating efficiency is high, improves
Gasification reaction accurately controls gasification reaction temperature by microwave heating, especially becomes apparent to the catalytic gasification reaction effect of coal；
The device that invention provides can be suitable for coal catalytic gasification destructive distillation coproduction and coal non-catalyzed gasification destructive distillation coproduction simultaneously.
(3), apparatus of the present invention are filled using high-temperature gasification synthesis gas as the fluidizing agent of fluidized bed dry distillation furnace and heat carrier
Divide the production for increasing combustion gas using the thermal energy in system, while avoiding using energy loss and formation caused by the cooling of water Quench
Contaminated wastewater；It decreases using boiler recycling heat bring investment and maintenance cost.
(4), gas-solid separator built in fluidized bed pyrolysis furnace includes that interconnected centrifugal deduster and filter element can use
The combustion gas dustiness of self-fluidized type bed pyrolysis oven is less than 8mg/Nm3, can be significant by fluidized bed pyrolysis furnace built in above-mentioned gas-solid separator
Ground reduces tar and results in blockage in the accumulation of filter element surface, extends filter element service life, due to fluidized bed dry distillation furnace
Interior top temperature is kept above 550 DEG C, and the tar in combustion gas is hardly agglomerated with fine ash.
(5), the synthesis gas coal gas processor for the first plasmatorch being equipped with by top is to by dedusting combustion gas hot tearing
Solution, the plasma of first 2500 DEG C of plasmatorch arc discharge output or more form tar in combustion gas, the heavy hydrocarbon pyrolysis
Small molecule fuel gas, increases fuel gases calorific value, and tar content is less than 5ppm in combustion gas after handling thermal cracking, can be directly used for
Engine or generator combustion power generation.
(6), boiler byproduct steam is set after synthesis gas coal gas processor as fluidized-bed gasification furnace gasifying agent, is realized
Thermal effect utilizes；Using the Partial cleansing combustion gas after recovered heat as fluidized-bed gasification furnace fluidizing agent, fluidized bed Jie is reduced
The investment of matter increases combustion gas active principle concentration and improves fuel gases calorific value.
(7), the cyclone separator of fluidized-bed gasification furnace includes concatenated first cyclone separator and the second cyclone separator
For depth separating high-temp synthesis gas entrained solid particle, gas solid separation operating pressure built in fluidized bed dry distillation furnace is reduced；
The coke recycle of the coarse granule of first cyclone separator separation and fluidized bed dry distillation fire grate Jiao Kou discharge is sent into fluidized gasification
Furnace gas improves charcoal percent conversion.More symmetrical openings are arranged on fluidized-bed gasification furnace scum pipe to be arranged obliquely
The second plasmatorch can generate 3000 DEG C or more flame of centre, fine ash that the second cyclone separator is isolated is sent into fluidized bed gas
The fine ash entrance changed on furnace slag discharge pipe is mixed with the clinker that slag-drip opening is discharged, and is melted under 3000 DEG C of conditions above, is passed through deslagging
Jet pipe that pipe is equipped with sprays into steam, and not only to have served as coolant cooling to slag but also serve as the carbon material of gasifying agent and melting and gasify to be formed
Synthesis gas.
(8), coal dust and gas in burner hearth are enhanced through the nozzle of setting tube-in-tube structure on fluidized-bed gasification furnace distribution grid
The mixed effect of agent avoids distribution grid near zone from forming dead zone, causes sintering damage distribution grid.The distribution of fluidized bed dry distillation furnace
Through setting jet pipe on plate, the turbulent closure scheme effect of coal dust and heat carrier in burner hearth is enhanced, homogeneous heating reduces the shape of tar
At.
Detailed description of the invention
Fig. 1 is that combined vaporizing destructive distillation of the invention prepares low tar gas combustion apparatus schematic diagram.
In figure, 1, gasification system；2, dry distillation of coal system；3, fluidized-bed gasification furnace；4, cyclone separator；5, slag collection
Device；6, furnace body；7, conical distribution plate；8, coal charge entrance；9, the burnt entrance of ash；10, shell；11, syngas outlet；12, microwave
Heating device；13, slag-drip opening；14, scum pipe；15, gas 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 furnace；2-2, gas-solid separator；2-3, synthesis gas coal gas processor；2-4,
First furnace body；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 tube；2-9, stream
Change gas distributing chamber；2-10, fluidizing gas blast pipe；2-11, the first plasmatorch；2-12, boiler；2-13, gas buffer are deposited
Storage tank；2-14, the first jet pipe.
Specific embodiment
Below with reference to the embodiments and with reference to the accompanying drawing the technical solutions of the present invention will be further described.
Embodiment 1: feed coal (lignite, anthracite or jet coal) water content after being dried is 6-10wt%, dehydration
Feed coal afterwards is crushed, sieving separating goes out to be greater than the broken coal B that 10mm is less than the broken coal A and 4-10mm of 16mm, broken coal B and catalysis
Agent is mixed to form Mixture Density Networks C, wherein catalyst is alkali or alkaline earth metal catalyst, and the mass ratio of broken coal B and catalyst is
80-200:1, Mixture Density Networks C are sent into fluidized-bed gasification furnace by the coal charge entrance 8 of fluidized-bed gasification furnace 3, preheated gasifying agent
(oxygen and steam) by the hole in furnace on the conical distribution plate 7 of 8 lower section of coal charge entrance and runs through through gasifying agent air inlet pipe 16
The nozzle 19 of the conical distribution plate 7 is sent into 3 burner hearth of fluidized-bed gasification furnace and fluidizes the Mixture Density Networks C, wherein control steam and coal
Mass ratio be 0.3-0.8:1, the mass ratio of oxygen and coal is 0.3-0.6:1, adjusts the power control of microwave heating equipment 12
Temperature in gasification furnace 3 at 700-850 DEG C, control furnace pressure be 0.1-0.4MPa, wherein gasification furnace body 6 top,
Middle part and lower part respectively set thermocouple, and the high-temperature synthesis gas that gasification is formed in gasification furnace 3 draws the furnace by syngas outlet 11
Body 6 is sent into the fluidizing gas blast pipe 2-10 of fluidized bed dry distillation furnace 2-1 after 4 dedusting of cyclone separator by pipeline, wherein
Cyclone separator 4 includes the first cyclone separator and the second cyclone separator being connected in series；High-temperature synthesis gas is through the fluidisation
The first conical distribution plate 2-5 of bed gas retort 2-1 and through the first conical distribution plate 2-5 jet pipe (2-14) for flowing
Change, heat and be sent into broken coal A through the first coal charge entrance 2-6, the combustion gas that destructive distillation generates is through being built in the fluidized bed dry distillation furnace 2-1's
It is closed after the gas-solid separator 2-2 purification at top, by being sent into the pipeline of gas-solid separator 2-2 top gas outlet connection
At bottle coal treatment apparatus 2-3；Wherein, the gas-solid separator 2-2 includes interconnected centrifugal deduster 2-12 and crosses filtering element
The multiple first plasmatorch 2-11 electric discharge output being arranged at the top of part 2-13, synthesis gas coal gas processor 2-3 is higher than 2500 DEG C
Tar in combustion gas, the heavy hydrocarbon pyrolysis are formed small molecule fuel gas by plasma, through synthesis bottle coal treatment apparatus 2-3 processing
Combustion gas afterwards is divided at least two parts, and a part of combustion gas is through pipeline to the gasification for not passing through flanged joint with the nozzle 19
Agent air inlet pipe 16 (outer tube preferably in the gasifying agent air inlet pipe 16 of cannula structure) enters the gas chamber 15 of gasification furnace 3, part combustion
Gas is used to fluidize the solid material in burner hearth through the hole on the conical distribution plate 7；A part of combustion gas is changed through boiler (2-12)
Gas buffer storage tank (2-13) is sent into after heat and byproduct steam.Wherein, the semicoke formed in fluidized bed dry distillation furnace 2-1 is through first
The coke discharging mouth 2-7 opened up in the middle part of conical distribution plate 2-5, the first coke discharging tube 2-8 being connected to the coke discharging mouth 2-7 are sent into the stream
Change the burnt entrance 9 of ash on bed gasification furnace 3；Wherein, the burnt entrance 9 of ash is to being placed in 8 lower section of coal charge entrance；Cyclone separator
The coarse granule that the first cyclone separator in 4 is isolated is sent into cycle gasification in gasification furnace 3 through the burnt entrance 9 of the ash；Second rotation
The fine ash that wind separator is isolated then is sent into the fine ash entrance 20 being arranged on the scum pipe 14 of fluidized-bed gasification furnace 3, fluidized bed gas
Change the lime-ash that the gasification of furnace 3 generates and the scum pipe 14, the lime-ash are entered by the slag-drip opening 13 opened up in the middle part of conical distribution plate 7
And fine ash passes through multiple second plasmatorch 17 being arranged below fine ash entrance 20 under the effect of gravity and forms high-temperature area heating
Melting, wherein described 3000 DEG C of second plasmatorch, 17 output or more flame of centre, a steam through boiler (2-12) by-product
Jet pipe 18 through being arranged below second plasmatorch 17 on the scum pipe 14 sprays into scum pipe 14, in thermodynamic activity
Under, the steam sprayed through jet pipe 18 is moved at V-type, and the steam flowed up in the lime-ash and fine ash of melting and scum pipe 14 is into one
Walk gasification reaction and form synthesis gas and enter in fluidized-bed gasification furnace 3 through scum pipe 14, in scum pipe 14 through just cooling slag into
Enter slag collection device 5；Wherein, the slag collection device 5 be tube-in-tube structure, can be made of inner barrel and outer barrel, outer cylinder with
Two groups of independent snakelike heat exchange tubes are set in the toroidal cavity of inner cylinder；Or it is made of inner cylinder, middle cylinder and outer cylinder, inner cylinder and middle cylinder
Between annular space flowing steam, annular space between outer cylinder and middle cylinder circulates oxygen；The O obtained through air-separating plant2And boiler
Another steam of (2-12) by-product respectively through the gas access on slag collection device 5 enter in heat exchange component with high temperature furnace slag
Heat exchange, the O after heating2It is respectively fed in the gasifying agent air inlet pipe 16 for passing through flanged joint with the nozzle 19 with superheated steam
Pipe and outer tube.Through detecting, carbon content is less than 4wt% in slag collection device 5, without synthesis gas coal gas processor 2-3 processing
Combustion gas tar content is greater than 1500ppm, and combustion gas tar content is less than 5ppm in gas buffer storage tank (2-13), and solid particle contains
Dust quantity is less than 8mg/Nm3, for coal treating capacity greater than 180 tons/d, system thermal efficiency is greater than 80%, and continuously-running 2 years stifled without tar
Plug filter element causes system shutdown.
Embodiment 2: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is identical, and difference is: broken coal B being directly sent into fluidized bed by the coal charge entrance 8 of fluidized-bed gasification furnace 3
Non-catalyzed gasification is carried out in gasification furnace, gasification temperature control is at 830-1150 DEG C.Through detecting, carbon contains in slag collection device 5
Amount is less than 3.85wt%, and the combustion gas tar content without synthesis gas coal gas processor 2-3 processing is greater than 1378ppm, gas buffer
Combustion gas tar content is less than 4.8ppm in storage tank (2-13), and solid particle dustiness is less than 7.8mg/Nm3, coal treating capacity is greater than
180 tons/d, system thermal efficiency is greater than 82%, and continuous operation 2 years is without blocking system shutdown caused by filter element because of tar.
Embodiment 3: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: the gas-solid separator 2-2 built in by fluidized bed dry distillation furnace is external, that is, passes through
Pipeline is connected to the outlet of fluidized bed dry distillation furnace furnace top gas, connecting tube road length 0.3-0.6m；Other technological parameters and 1 phase of embodiment
Together, system shutdown caused by being blocked because of filter element tar for system continuous operation 13 months.
Embodiment 4: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: the gas-solid separator 2-2 built in fluidized bed dry distillation furnace be two it is concatenated from
Heart deduster, other technological parameters are same as Example 1.Through detecting, carbon content is less than 4wt% in slag collection device 5, without
The combustion gas tar content of synthesis gas coal gas processor 2-3 processing is greater than 1760ppm, and combustion gas contains in gas buffer storage tank (2-13)
Tar content is less than 6.5ppm, and solid particle dustiness is greater than 169mg/Nm3, for coal treating capacity greater than 180 tons/d, system thermal efficiency is big
In 80%, system shutdown is caused without tar blocking filter element within continuously-running 2 years.
Embodiment 5: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: the gas-solid separator 2-2 built in fluidized bed dry distillation furnace is two concatenated mistakes
Original part is filtered, other technological parameters are same as Example 1.System shutdown caused by being blocked because of filter element for system continuous operation 6 months.
Embodiment 6: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: the fine ash that the second cyclone separator separates equally being passed through grey burnt entrance 9 and is sent into stream
Change bed gasification furnace, other technological parameters are same as Example 1.Through detecting, less than 74%, system is run 11 months system thermal efficiency
System shutdown caused by being blocked because of filter element；Carbon content is less than 4wt% in slag collection device 5, without the processing of synthesis gas coal gas
The combustion gas tar content of device 2-3 processing is greater than 1500ppm, and combustion gas tar content is less than in gas buffer storage tank (2-13)
5ppm, solid particle dustiness are less than 8mg/Nm3, for coal treating capacity greater than 180 tons/d, system thermal efficiency, can be continuous less than 74%
System shutdown is caused without tar blocking filter element within operation 2 years.
Embodiment 7: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: the second plasmatorch is not provided on fluidized-bed gasification furnace scum pipe, by the second whirlwind
The fine ash of separator separation is sent into fluidized-bed gasification furnace by the burnt entrance 9 of ash, and other technological parameters are same as Example 1.Through examining
It surveys, carbon content is greater than 10wt% in slag collection device 5, and carbon utilisation rate is low.
Embodiment 8: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: is not set on fluidized-bed gasification furnace conical distribution plate 7 through the conical distribution plate
Nozzle 19, that is, the gasifying agent (oxygen and superheated steam) after preheating and the part circulating gas for serving as fluidizing agent pass through gas
Agent air inlet pipe 16 enters gasification furnace burner hearth, other technological parameters and 1 phase of embodiment through the hole on the conical distribution plate 7
Together.Through detecting, carbon content is less than 4.5wt% in slag collection device 5, and system runs 14 months fluidized-bed gasification furnace conical distributions
Hardened slag is serious, and system is caused to be forced to stop.
Embodiment 9: the embodiment carries out that combined vaporizing destructive distillation prepares the method for low tar combustion gas and embodiment 1 is carried out
The device of method selection is different, and difference is: fluidized-bed gasification furnace slag collection device 5 be non-tube-in-tube structure, i.e. gasifying agent not
It is sent directly into gasifying agent air inlet pipe 16 through the heat exchange recycling heat of slag collection device 5, other technological parameters are same as Example 1.
Through detecting, system thermal efficiency is less than 50%, and carbon content is less than 4.1wt% in slag collection device 5, without the processing of synthesis gas coal gas
The combustion gas tar content of device 2-3 processing is greater than 1700ppm, and combustion gas tar content is less than in gas buffer storage tank (2-13)
5.3ppm, solid particle dustiness are less than 10mg/Nm3, coal treating capacity is greater than 180 tons/d, and continuously-running 2 years without tar blocking
Filter element causes system shutdown.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., is all included in the scope of protection of the present invention.
Claims (14)
1. a kind of combined vaporizing destructive distillation prepares low tar gas combustion apparatus, including gasification system (1) and dry distillation of coal system (2),
Be characterized in that: the gasification system (1) include: fluidized-bed gasification furnace (3), cyclone separator (4), slag collection device (5) and
Gasifying agent supply system；The fluidized-bed gasification furnace (3) includes the cone of furnace body (6) and the interior lower part setting of shell (10), furnace body (6)
The burnt entrance (9) of coal charge entrance (8) and ash being arranged above shape distribution grid (7), the conical distribution plate (7)；The fluidized bed
The setting of gasification furnace (3) top runs through the syngas outlet (11) of the furnace body (6) and shell (10), furnace body (6) and shell (10)
Microwave heating equipment (12) are set in the toroidal cavity of formation, the microwave heating equipment (12) is arranged in conical distribution plate (7)
Between syngas outlet (11)；It is opened up slag-drip opening (13) in the middle part of conical distribution plate (7), slag-drip opening (13) passes through scum pipe (14)
It is connected to slag collection device (5)；Gas chamber (15) are formed between shell (10) lower head below the conical distribution plate (7),
Gasifying agent air inlet pipe (16) is arranged through the shell (10) and furnace body (6)；
The dry distillation of coal system (2) includes fluidized bed dry distillation furnace (2-1), gas-solid separator (2-2) and synthesis gas coal gas processor
(2-3)；The fluidized bed dry distillation furnace (2-1) includes the first furnace body (2-4), the interior lower part setting first of the first furnace body (2-4)
Conical distribution plate (2-5), the first coal charge entrance (2-6) that the first conical distribution plate (2-5) top is arranged；First taper point
It is opened up coke discharging mouth (2-7) in the middle part of fabric swatch (2-5), the coke discharging mouth (2-7) passes through the first coke discharging tube (2-8) and the burnt entrance of the ash
(9) it is connected to；Fluidizing gas distributing chamber (2- is formed below first conical distribution plate (2-5) between the first furnace body (2-4) inner wall
9)；The fluidizing gas air inlet being connected to the fluidizing gas distributing chamber (2-9) is set on the first furnace body (2-4) outer wall
It manages (2-10)；The gas-solid separator (2-2) is built at the top of the fluidized bed dry distillation furnace (2-1), the gas-solid separator (2-
2) gas vent is connected to by pipeline with synthesis gas coal gas processor (2-3) air inlet；At the top of synthesis gas coal gas processor (2-3)
3-5 the first plasmatorch (2-11), place's synthesis gas coal gas processor (2-3) gas vent and gas buffer storage tank are set
(2-13) connection；
Cyclone separator (4) air inlet and air outlet are entered the wind with the syngas outlet (11) and the fluidizing gas respectively
Manage (2-10) connection；Cyclone separator (4) the solids discharge mouth and the burnt entrance (9) of the ash.
2. combined vaporizing destructive distillation according to claim 1 prepares low tar gas combustion apparatus, it is characterised in that: the fluidized bed
Two symmetrical the second plasmatorch (17), and the second plasmatorch are additionally provided on the scum pipe (14) of gasification furnace (3)
(17) it is arranged obliquely with scum pipe (14) axis at 30-60 degree angle opening.
3. combined vaporizing destructive distillation according to claim 2 prepares low tar gas combustion apparatus, it is characterised in that: described second etc.
Ion torch (17) is arranged with the scum pipe (14) axis at 45 degree of angle openings obliquely.
4. combined vaporizing destructive distillation according to claim 1 prepares low tar gas combustion apparatus, it is characterised in that: the gas-solid point
It include the centrifugal deduster and filter element being arranged in series from device (2-2).
5. combined vaporizing destructive distillation according to claim 4 prepares low tar gas combustion apparatus, it is characterised in that: described to cross filtering element
Part is ceramic porous material or iron aluminum metal sintered porous material.
6. combined vaporizing destructive distillation according to claim 1 prepares low tar gas combustion apparatus, it is characterised in that: the synthesis gas
The first plasmatorch (2-11) Cheng Yuanzhou being arranged at the top of coal gas processor (2-3) is arranged symmetrically.
7. combined vaporizing destructive distillation according to claim 6 prepares low tar gas combustion apparatus, it is characterised in that: described first etc.
The quantity of ion torch (2-11) is 4, and first plasmatorch (2-11) and the synthesis gas coal gas processor (2-3) are vertical
Azimuth axis is arranged obliquely at 45 degree of angle openings.
8. combined vaporizing destructive distillation described in any one of -4 claims prepares low tar gas combustion apparatus according to claim 1, special
Sign is: the slag collection device (5) is the tube-in-tube structure being made of inner cylinder, middle cylinder and outer cylinder, and inner cylinder collects clinker, inner cylinder
Annular space flowing steam between middle cylinder, the annular space circulation oxygen between outer cylinder and middle cylinder.
9. combined vaporizing destructive distillation according to claim 5 prepares low tar gas combustion apparatus, it is characterised in that: the whirlwind point
From device (4) include the first cyclone separator and the second cyclone separator, the syngas outlet (11), the first cyclone separator,
Second cyclone separator is sequentially connected, and the air inlet of the second cyclone separator and gas outlet go out with the first cyclone separator respectively
Port is connected to the fluidizing gas blast pipe (2-10) in dry distillation of coal system (2)；The first cyclone separator solid goes out
Material mouth is connected to the burnt entrance (9) of the ash, and the second cyclone separator solid fine ash discharge port and setting are in the scum pipe
(14) fine ash entrance (20) connection on, the fine ash entrance (20) are located above the second plasmatorch (17).
10. combined vaporizing destructive distillation described in any one of -7,9 claims prepares low tar gas combustion apparatus according to claim 1,
Be characterized in that: the quantity of the gasifying agent air inlet pipe (16) of the fluidized-bed gasification furnace (3) is 4 and, institute symmetrical at circumference
Stating gasifying agent air inlet pipe (16) is to be made of inner tube with the outer tube being set in outside inner tube, through the conical distribution plate (7) setting 2
It is a to be located on same circumference and symmetrically arranged nozzle (19), nozzle (19) nozzle are by inner tube and being set in outside inner tube
The tube-in-tube structure of outer tube composition, nozzle (19) central inner pipe front end face distance L between its outer tube front end face is 20-
35mm, the nozzle (19) are connect by flange with gasifying agent air inlet pipe (16) compartment of terrain.
11. a kind of method that combined vaporizing destructive distillation prepares low tar combustion gas, it is characterised in that: the described method includes: (a), be mixed with
Catalyst or the coal dust for not being mixed with catalyst are sent into gasification furnace (3) furnace through the coal charge entrance (8) of fluidized-bed gasification furnace (3)
Thorax, the gasifying agent of preheating are sent into gasification furnace (3) burner hearth through the conical distribution plate (7) of the fluidized-bed gasification furnace (3) and are fluidized
The coal dust, the microwave in furnace body (6) and shell (10) toroidal cavity of the heat needed for coal dust gasification by being located at gasification furnace (3)
Heating device (12) provides, and the high-temperature synthesis gas formed in fluidized-bed gasification furnace (3) passes through the synthesis gas on the gasification furnace (3)
(11) are exported to draw；(b), high-temperature synthesis gas fluidisation through fluidized bed dry distillation furnace (2-1) after cyclone separator (4) processing
Gas blast pipe (2-10) and the first conical distribution plate (2-5) enter fluidized bed dry distillation furnace (2-1) burner hearth for serving as stream
Change medium and heat carrier make by be located at the first coal charge entrance (2-6) being arranged above the first conical distribution plate (2-5) into
Enter powder fluidized in fluidized bed dry distillation furnace (2-1) burner hearth, destructive distillation forms combustion gas, the combustion gas is through fluidized bed dry distillation furnace
Synthesis gas coal gas processor (2-3) is sent into after gas-solid separator (2-2) dedusting built in (2-1) furnace roof；(c), synthesis gas coal gas
The first plasmatorch (2-11) being arranged at the top of processor (2-3) is made by 2500 DEG C of arc discharge output or more of plasma
Tar in combustion gas, the heavy hydrocarbon pyrolysis form small molecule fuel gas, through synthesis bottle coal treatment apparatus (2-3) treated combustion gas
It is divided at least two parts, a part introduces the fluidized-bed gasification furnace (3) for coal charge in fluidized furnace, and another part is through boiler
(2-12) is sent into gas buffer storage tank (2-13) after recycling heat byproduct steam.
12. the method that combined vaporizing destructive distillation according to claim 11 prepares low tar combustion gas, it is characterised in that: the side
Method prepares low tar gas combustion apparatus using combined vaporizing destructive distillation described in any one of claim 1-10 claim and implements.
13. the method that combined vaporizing destructive distillation according to claim 12 prepares low tar combustion gas, it is characterised in that: gasification temperature
Degree is 700-850 DEG C, vapor pressure 0.1-0.4MPa, and the mass ratio of steam and coal is 0.3-0.8:1 in gasification furnace, oxygen with
The mass ratio of coal is 0.3-0.6:1.
14. the method that combined vaporizing destructive distillation according to claim 13 prepares low tar combustion gas, it is characterised in that: gasification temperature
Degree is 780-820 DEG C, vapor pressure 0.25-0.35MPa, and the mass ratio of steam and coal is 0.5-0.7:1, oxygen in gasification furnace
Mass ratio with coal is 0.4-0.5:1.
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| CN116590056A (en) * | 2017-01-17 | 2023-08-15 | 北京科立科盈科技有限公司 | Preheating system and preheating method of gasifying agent for fluidized bed gasifier |
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| CN104178224A (en) * | 2014-08-07 | 2014-12-03 | 新奥科技发展有限公司 | Gas distributor, gasifier and carbon-containing material gasification method |
| CN104711003A (en) * | 2015-03-13 | 2015-06-17 | 东南大学 | Device and method for utilizing biological substance for monobed self-heating oil manufacturing with coke separation function |
| CN105505467A (en) * | 2015-12-04 | 2016-04-20 | 中国天辰工程有限公司 | Coupling technology adopting lignite-gasification gas production and dry distillation upgrading |
| CN105368497A (en) * | 2015-12-11 | 2016-03-02 | 山东百川同创能源有限公司 | Biomass material microwave-assisted pyrolysis gasification device, and application method thereof |
| CN206033675U (en) * | 2016-07-13 | 2017-03-22 | 陕西首信实业有限公司 | Low tar gas device of dry distillation of jointly gasifying preparation |
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