CN104479748B - Coal gasifier - Google Patents
Coal gasifier Download PDFInfo
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- CN104479748B CN104479748B CN201410557701.5A CN201410557701A CN104479748B CN 104479748 B CN104479748 B CN 104479748B CN 201410557701 A CN201410557701 A CN 201410557701A CN 104479748 B CN104479748 B CN 104479748B
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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
- C10J3/723—Controlling or regulating the gasification process
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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
- C10J3/466—Entrained flow processes
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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
- C10J3/485—Entrained flow gasifiers
- C10J3/487—Swirling or cyclonic gasifiers
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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
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
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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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
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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
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
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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
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
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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
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
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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
- C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
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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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
Abstract
The coal gasifier of the present invention possesses：Reaction vessel (12), it is formed as the cylindrical shape extended upward and is provided with outlet in upper end side；The burner nozzle (17) of tubular, its with plane-parallel and on inner peripheral surface in reaction vessel on the datum plane (P1) of the lower section of outlet it is spaced apart in the circumferential direction be positioned apart from it is multiple, and coal and oxidant are supplied into reaction vessel, at least manufactured in the coal gasifier of hydrogen and CO gas by making coal be burnt in reaction vessel, each burner nozzle by it is viewed from above when itself axis (C1) it is smaller than the internal diameter of reaction vessel with diameter and imaginary circle centered on central axis is tangent around same direction, and the axis of itself and plane-parallel more configure towards the front end of burner nozzle mode more downward.
Description
It is on April 11st, 2011, the Chinese Application No. of entitled " coal gasifier " applying date that the application, which is,
201180019197.8 divisional application.
Technical field
The present invention relates to coal gasification is produced into the coal gasifier of imflammable gas with oxidants such as oxygen, vapor.
The Japanese Patent Application 2010-095496 claims priorities that the application is filed an application based on April 16th, 2010 in Japan
Power, and here cite its content.
Background technology
In the past, as producing the gasification furnace (coal gasifier) of imflammable gas by fine coal etc., such as known there is patent document 1
Shown gasification furnace.In the gasification furnace, in the pressure vessel (reaction vessel), 4 combustion furnace burners during top view
(combustor burner) is equidistantly configured on the circumference in defined plane.Also, clip the central shaft of circumference and
The 2 groups of combustion furnace burners configured on symmetrical position are configured in a manner of mutually opposing.
Combustion furnace burner by centrally disposed portion and for start gasification furnace light oil burner, with light oil burner be in concentric circles
The air nozzle that is configured successively by Inside To Outside, coal tar nozzle, fuel coal nozzle, auxiliary air nozzle are formed shape.
Air, coal tar (unvaporized coal residue or pyrolysis residue), fuel coal are after respective nozzle internal rotation, by light oil
Burner is lighted and sprayed into pressure vessel.
Prior art literature
Patent document
Patent document 1：No. 3595404 publications of Japanese Patent No.
The content of the invention
Invention technical problems to be solved
But problems be present in the gasification furnace shown in above-mentioned patent document 1：Sprayed when from each combustion furnace burner
During gas of rotational flow etc., because the configuration of combustion furnace burner is sprayed on mutually opposing position, therefore from combustion furnace burner
Gas gone out etc. can be collided mutually, the flowing instability of gas in gasification furnace etc..Also, the inner peripheral surface of gasification furnace is because of the portion of coal
Divide oxidation (hereinafter referred to as " gasifying ") and be exposed under hot environment, if not adhering to one stably on the inner peripheral surface of gasification furnace
Determine the clinker of thickness, then there is a possibility that following：Not only heat loss becomes causes performance to reduce greatly, and the inner peripheral surface can also be by
Damage is produced to the influence of heat.
And then can be risen by gas caused by gasification etc. in gasification furnace, but when the rising of the gas in gasification furnace etc.
When flowing produces uneven, the carbon in coal (coal tar) fully occurs to flow out from gasification furnace before gasification reaction sometimes, makes anti-
Should rate (conversion ratio that the carbon in coal converts to gas) reduction.
The present invention is to complete in view of the above problems, and its object is to provide a kind of to make coal in compact reaction
Fully reacted in container and clinker is stably adhered to the efficient coal gasification on the inner peripheral surface of reaction vessel
Stove.
For solving the means of technical problem
In order to solve the above-mentioned technical problem, the present invention proposes following means.
The coal gasifier of the present invention possesses：
Reaction vessel, it is formed as the cylindrical shape extended upward and is provided with outlet in upper end side；With
The burner nozzle of tubular, its with plane-parallel and positioned at above-mentioned outlet lower section datum plane on described
It is spaced apart in the circumferential direction on the inner peripheral surface of reactor to be positioned apart from multiple, and coal and oxidation are supplied into above-mentioned reaction vessel
Agent,
In the coal gasifier, hydrogen and an oxygen are at least manufactured by making above-mentioned coal gasify in above-mentioned reaction vessel
Change carbon gas,
Characterized in that, each above-mentioned burner nozzle with it is viewed from above when the axis of itself and diameter than above-mentioned reaction vessel
Internal diameter is smaller and imaginary circle centered on above-mentioned central axis is tangent around same direction and the axis of itself with it is horizontal
Face is parallel or is more configured towards the front end of above-mentioned burner nozzle mode more downward.
I.e., in the present invention, hydrogen and CO gas are at least manufactured by making coal gasify in reaction vessel
Coal gasifier is characterised by that it has：
Reaction vessel, it is formed as the cylindrical shape extended upward；
Outlet, it is arranged on the upper end side of above-mentioned reaction vessel；With
The burner nozzle of multiple tubulars, it supplies coal and oxidant into above-mentioned reaction vessel,
Above-mentioned multiple burner nozzles are on the datum plane with plane-parallel positioned at the lower section of above-mentioned outlet towards upper
The circumferencial direction for stating the inner peripheral surface of reaction vessel is set at spaced intervals,
The axis of above-mentioned each burner nozzle and the center with above-mentioned reaction vessel when being observed with the top of container from the reactions above
Centered on axis and imaginary circle that diameter is smaller than the internal diameter of reaction vessel is above-mentioned to configure around the tangent mode of same direction
Each burner nozzle,
Above-mentioned burner nozzle with the axis of above-mentioned burner nozzle and plane-parallel or more towards the front end of above-mentioned burner nozzle more
Mode downward configures.
According to the present invention, when burner nozzle supplies coal and oxidant into the reaction vessel of cylindrical shape, it can produce and surround
The flowing of the fluid of the central axis rotation of reaction vessel.Therefore, the flowing of the fluid near the inner peripheral surface of reaction vessel is in circle
The optional position of circumferential direction is stable, can make to be attached on the inner peripheral surface of reaction vessel because of coal gasification and caused by melt
The thickness of clinker is generally uniform.
In addition, burner nozzle with the axis of itself and plane-parallel or more towards the front end of burner nozzle more downward
Mode configures.By expand gasification and reaction vessel inner edge rotate coal that side rises from burner nozzle first to it is horizontal or under
Fang Liudong, so as to increase the time that coal flows in reaction vessel, make it before outlet discharge in reaction vessel
It is fully vaporization.
In addition, in above-mentioned coal gasifier, above-mentioned burner nozzle is more preferably between central axis of above-mentioned reaction vessel etc.
Configured every ground.
In accordance with the invention it is possible to make including from the coal and oxidant of burner nozzle supply and because of coal in reaction vessel
Burning and the flowing of the fluid of caused gas is more stable.
In addition, in above-mentioned coal gasifier, above-mentioned imaginary diameter of a circle relative to the internal diameter of above-mentioned reaction vessel ratio more
It is preferably set to more than 1/10 and less than 1/3.
According to the present invention, pass through the ratio (hereinafter also referred to " diameter by imaginary diameter of a circle relative to the internal diameter of reaction vessel
Than ") less than 1/3 is set to, the velocity gradient of the fluid on the inner peripheral surface of reaction vessel can be reduced, suppression is attached to reaction vessel
Inner peripheral surface on clinker from inner peripheral surface peel off.Therefore, it is possible to prevent the inner peripheral surface of reaction vessel to be exposed under high temperature because of heat
The increase of loss and cause performance reduce or inner circumferential surface damage.
In addition, by the way that diameter ratio is set into more than 1/10, can prevent from the coal of burner nozzle supply and oxidant etc. mutually
Generation head-on crash, the flowing rotated around the central axis of reaction vessel is positively produced, makes the gasification reaction time elongated, carries
High reactivity.
In addition, in above-mentioned coal gasifier, it is above-mentioned when will be supplied from each above-mentioned burner nozzle into above-mentioned reaction vessel
Coal, the mass flow of above-mentioned oxidant are set to m1 (kg/s), m2 (kg/s), by the above-mentioned coal in each above-mentioned burner nozzle, above-mentioned
When the flow velocity of oxidant is set to V1 (m/s), V2 (m/s), the mean flow rate Va (m/s) obtained by (1) formula is more preferably set as 10
(m/s) more than and 50 (m/s) below.
Va=(m1 × V1+m2 × V2)/(m1+m2) (1)
According to the present invention, by the way that mean flow rate Va is set into 50 (m/s) below, can suppress to be attached to the interior of reaction vessel
Clinker on side face peels off from inner peripheral surface, so as to reduce the heat loss from reaction vessel to exterior conductive.In addition, pass through by
Mean flow rate Va is set to more than 10 (m/s), can stably transmit coal using oxidant in burner nozzle.
In addition, in above-mentioned coal gasifier, the angle of the axis of each above-mentioned burner nozzle with respect to the horizontal plane is more preferably set
It is set to more than 0 ° and less than 10 °.
According to the present invention, by the way that the angle is set into more than 0 ° and less than 10 °, the coal particle being blown into from burner nozzle can be made
High temperature director's time near burner nozzle is present, so that the gasification reaction of coal tar is promoted, it is possible to increase reactivity.
In addition, in above-mentioned coal gasifier, the nearest top of above-mentioned burner nozzle more preferably in above-mentioned reaction vessel and
Coal tar burner is set in the same manner as above-mentioned burner nozzle on the second datum plane parallel with said reference plane.
According to the present invention, the coal tar for being recovered unreacted by using the coal tar burner of reaction vessel is reused in coal
Gasification furnace simultaneously brings it about gasification reaction, and the gasification reaction rate that can make the carbon in coal is more than 99%.
Invention effect
According to the coal gasifier of the present invention, coal can be made fully to be reacted in compact reaction vessel, and energy
Enough clinker is set to be stably adhered on the inner peripheral surface of reaction vessel.
Brief description of the drawings
Fig. 1 is the block diagram of the synthesis gas from coal gasification body manufacture system for the coal gasifier for having used embodiment of the present invention.
Fig. 2 is the profilograph of the major part of the coal gasifier of embodiment of the present invention.
Fig. 3 is the top plan view along the line of cut A-A in Fig. 2.
Fig. 4 is the figure for the velocity flow profile for representing the datum plane in Fig. 3.
Fig. 5 be the coal gasifier for representing embodiment of the present invention partial oxidation portion in heat loss ratio and reactivity ratio with it is straight
The figure of relation between the ratio of footpath.
Fig. 6 be in the coal gasifier for represent embodiment of the present invention heat loss than between coal and the mean flow rate of oxidant
Relation figure.
Embodiment
Hereinafter, the embodiment of the coal gasifier of the present invention is illustrated while referring to figs. 1 to Fig. 6.Coal gasifier is
It is assembled into a part for gasification system to use and by making coal internally burn at least to manufacture hydrogen and carbon monoxide
The device of gas.
As shown in figure 1, synthesis gas from coal gasification body manufacture system 1 is to be manufactured using coal as raw material with hydrogen and carbon monoxide
Complete set of equipments of the gas as the forming gas of principal component.By the original that the product forming gas is used as to chemical synthesis equipment etc.
Material is supplied, and can finally manufacture methane, methanol and ammonia etc..
Synthesis gas from coal gasification body manufacture system 1 possesses coal and crushed and drying equipment 2, coal supply arrangement 3, present embodiment
Coal gasifier 4, heat recovery equipment 5, coal tar reclaimer 6, transformationreation equipment 7, gas refinishing equipment 8 and air separation equipment
9。
Generally, the external diameter of coal is uneven, according to its species sometimes with the moisture more than desired value.Therefore, first
Coal crush and drying equipment 2 in, coal is crushed, below 200 mesh is 75% or so, average grain diameter as 30~60 to be formed
(μm) left and right fine coal, be then dried, with reach defined moisture, preferably with total moisture gauge reach 10% with
Under, it is then supplied to coal supply arrangement 3.In addition, after coal crushing and drying equipment 2 untill coal gasifier 4, in order that dry
The amount of moisture in coal after dry does not change, and coal moves in closed space.
Then, in order to supply coal into coal gasifier 4, defined pressure is boosted to using carrier gas etc. in coal supply arrangement 3
After power, the coal to the weight feed predetermined weight of coal gasifier 4 is transmitted by air-flow.The operating pressure of coal gasifier does not limit especially
It is fixed, but from the viewpoint of raising, installation cost and the charges for water and electricity of the reaction efficiency brought from gasification furnace densification reduce, be preferably
More than 2MPaG and below 5MPaG.
On the other hand, air compression is made it liquefy and utilizes the difference of boiling point from as liquid by air separation equipment 9
Dry oxygen and nitrogen etc. are separated in air afterwards.The oxygen isolated from air separation equipment 9 is with regulation flow to coal gas
Change stove 4 to supply.
As shown in Fig. 2 up D1 at least has partial oxidation portion (reaction vessel) 12 to coal gasifier 4, in partial oxidation
The lower section D2 in portion 12 is provided with preheating part 15.Partial oxidation portion 12 and preheating part 15 connect on above-below direction D.
As shown in Figures 2 and 3, by using formation such as the refractory bodies of heat resistance, D prolongs along the vertical direction in partial oxidation portion 12
The cylindrical shape stretched, on the inner peripheral surface in partial oxidation portion 12, provided with cylindric 8 burner nozzle for being formed as extending along axis C1
17a~17h (it is following, when no special difference earth's surface shows these burner nozzles 17a~17h, they are referred to as " burner nozzle
17”)。
In addition, the quantity of the burner nozzle 17 to being arranged in partial oxidation portion 12 does not limit, as long as more than 2 how much
It is individual can.Wherein, preferably with partial oxidation portion 12 size become greatly by 4,6,8 ... increase in a manner of such
Even number is arranged to quantity, even if being that odd number also has no problem completely.
8 burner nozzles 17 are arranged on the datum plane P1 with plane-parallel, and the center of surrounding portion oxidation section 12
Axis C2 is equally spaced configured.
On burner nozzle 17, as shown in figure 3, during with from the D1 of top the axis C1 of burner nozzle 17 with diameter than part oxygen
The internal diameter R1 in change portion 12 is smaller and imaginary circle E centered on central axis C2 around same direction F1 it is tangent in a manner of match somebody with somebody
Put.Here, refer to around same direction F1 is tangent, prolong when the axis C1 of each burner nozzle 17 is considered as from the front end of burner nozzle 17
During the line stretched, axis C1 is tangent around direction F1 relative to imaginary circle E.Alternatively, it is also possible to the axis C1 of each burner nozzle 17
Configured with imaginary circle E around the direction opposite with direction F1 is the tangent modes of direction F2.
Also, relative to the internal diameter R1 in partial oxidation portion 12 ratio, (imaginary diameter of a circle R2/ is anti-with imaginary diameter of a circle R2
Answer the internal diameter R1 of container) i.e. diameter set than reaching the mode of more than 1/10 and less than 1/3.Diameter ratio more preferably 1/5
Above and less than 3/10.
And then as shown in Fig. 2 with the angle, θs of the axis C1 of burner nozzle 17 with respect to the horizontal plane reach more than 0 ° and 10 ° with
Under mode set.
That is, inclined downward of the front end of burner nozzle 17 preferably to partial oxidation portion 12 and with respect to the horizontal plane for more than 0 ° and
Less than 10 °, more preferably more than 0 ° and less than 2 °.
It is crushed in coal crushing and drying equipment 2 with the coal of dried micro mist shape by coal supply unit 20 with defined stream
Amount is supplied to each burner nozzle 17.The oxygen isolated by air separation equipment 9 and supplied as described later by heat recovery equipment 5
Vapor each burner nozzle 17 is supplied to defined flow by oxidant supply unit 21.
More specifically, by the coal being supplied to from burner nozzle 17 in partial oxidation portion 12, oxidant (oxygen and vapor)
Mass flow is set to m1 (kg/s), m2 (kg/s), and coal, the flow velocity of oxidant in burner nozzle 17 are set into V1 (m/s), V2 (m/
s).Now, reached more than 10 (m/s) with the mean flow rate Va (m/s) obtained by following (2) formulas and the sides of 50 (m/s) below
Formula, the flow of coal and oxidant is adjusted by coal supply unit 20 and oxidant supply unit 21.
Va=(m1 × V1+m2 × V2)/(m1+m2) (2)
That is, mean flow rate Va refers to the mean flow rate of the fluid from the raw material jet injection of burner nozzle 17.
Wherein, the oxygen in oxidant is in the range of being calculated as 0.7~0.9 with the weight of oxygen and coal ratio (oxygen/coal), water steaming
Gas in the range of being calculated as 0.05~0.3 with the weight of vapor and coal ratio (vapor/coal), according to coal kind and operating plan
Temperature is suitably set.In addition, the flow velocity V1 (m/s) of the oxidant in burner nozzle 17 is set to oxygen and vapor mixing
Flow velocity in the state of afterwards.On the difference of coal kind, can with the Analysis Values and elemental analysis value of coal, ash composition etc. come
Represent.
In addition, mean flow rate Va be more preferably more than 10 (m/s) and 30 (m/s) below.
On the outer peripheral face in partial oxidation portion 12, the cooling wall pipeline 22 for cooling segment oxidation section 12 is equipped,
The pump 23 for flowing into water or saturation water (boiler water) to its inside is connected with cooling wall pipeline 22.In the cooling wall pipeline 22
The water or saturation water of interior flowing can circulate in cooling wall pipeline 22, partial oxidation portion 12 can also be used as into boiler to carry out
Heating, vapor recovery and utilization are used as after forming the vapor of high temperature.
Coal and oxidant after being crushed and boosting are supplied to partial oxidation portion with mean flow rate Va from above-mentioned burner nozzle 17
In 12.8 burner nozzles 17 due to configuring as shown in Figure 3, therefore the coal and oxidant that are supplied from burner nozzle 17 are as shown in Figure 2
Like that, first with skirt around the side that the central axis C2 rotations side in partial oxidation portion 12 is downward or is flowed in same level
Formula is sprayed.Being changed into high temperature and high pressure in partial oxidation portion 12, (such as temperature is more than 1200 DEG C and less than 1800 DEG C, pressure is
More than 2MPa).In the present context, coal becomes the concurrent heat solution of high temperature, coal tar and the volatility gas for including tar and vapor etc.
Body separates, and at the same time coal gasifies, so as to produce an oxygen of the high temperature based on following chemical equations (1)~(3)
Change carbon gas, carbon dioxide and hydrogen and clinker (ash content).
2C+O2→2CO (1)
C+O2→CO2 (2)
C+H2O→CO+H2 (3)
Now the velocity flow profile of hydrogen and CO gas etc. is shown in Fig. 4 in each position in partial oxidation portion 12.Fig. 4
It is to represent on the datum plane P2 of the central axis C2 comprising partial oxidation portion 12 shown in Fig. 3 from central axis C2 to r side
To position flow velocity v figure.Here, datum plane P2 is relative to the face vertical with the datum plane P1 of plane-parallel.
In partial oxidation portion 12, the fluid such as hydrogen and CO gas from central axis C2 to radial direction (r directions) skirt around
Same direction (such as direction F1) rotation side rises.Fig. 4 shows r directions on the position of datum plane P2 some height
The flow velocity v of fluid change (distribution).Here, the position of some height refers to along any of the short transverse in partial oxidation portion 12
Position, as long as on burner nozzle 17a.In Fig. 4, transverse axis represents the position in the r directions relative to central axis C2, indulges
Axle represents flow velocity v.In addition, actually the position in r directions is at positive side (in Fig. 3 relative to central axis C2 be burner nozzle 17a sides)
When at minus side (in Fig. 3 relative to central axis C2 be burner nozzle 17e sides), flow velocity v direction is different from the position in r directions
, but Fig. 4 illustrate only flow velocity v size without considering its direction.In addition, Fig. 4 does not consider to be attached to partial oxidation portion 12
Inner peripheral surface on aftermentioned clinker thickness.
In Fig. 4, it is indicated by the solid line with imaginary diameter of a circle relative to partial oxidation portion (reaction vessel) 12 internal diameter it
Mode than reaching more than 1/5 and less than 3/10 sets burner nozzle 17 in partial oxidation portion 12 and is set to mean flow rate Va
More than 10 (m/s) and flow velocity v when 30 (m/s) are below model.
In Fig. 4, as shown by the solid line, the position on burner nozzle 17c axis C1 is that the position in r directions is R2/2 position
It is near-R2/2 position to put the position i.e. position in r directions nearby and on burner nozzle 17g axis C1, and flow velocity v is maximum.And
And the position of the inner peripheral surface in partial oxidation portion 12 be r directions position be R1/2 position and for-R1/2 position, flow velocity
V is close to 0, and the absolute value of flow velocity v slope of a curve (velocity gradient) is changed into less value.
When hydrogen and CO gas etc. are assumed to be into Newtonian fluid, the power (shearing force) that fluid attempts to peel off clinker is
The flow velocity v of fluid velocity gradient is multiplied by value obtained by the viscosity μ of fluid (μ (dv/dr)), it may thus be appreciated that shearing now
Power is smaller.
On the other hand, in the comparative example that the mean flow rate Va obtained by (2) formula has exceeded 50 (m/s), such as dotted line in Fig. 4
Shown, flow velocity v is that the position of maximum is constant, but flow velocity v maximum increase.Therefore, flow velocity v slope of a curve is absolute
Value increase, acts on the shearing force increase of clinker, and clinker becomes easily to peel off.
In addition, the composition in the partial oxidation portion 12 relative to the velocity flow profile for showing fluid shown in solid, makes burner
Portion 17b axis C1 leaves from the central axis C2 in partial oxidation portion 12 and makes diameter than in the comparative example more than 1/3, fluid
Velocity flow profile be changed into Fig. 4 distribution shown in double dot dash line.I.e., in this case, also due to partial oxidation portion 12
The position of inner peripheral surface is the absolute value increase of the slope of a curve for the flow velocity v that the position in r directions is R1/2 and-R1/2 opening position
And make the shearing force increase for acting on clinker, therefore clinker also becomes easily to peel off.
As shown in Fig. 2 in partial oxidation portion 12 the caused equilateral surrounding portion oxidation section 12 of gas and clinker center
Axis C2 rotates side to movement on the outside of the direction of footpath, and is changed into high temperature and expands such that in the presence of buoyancy by upward
Power and partial oxidation portion 12 inner peripheral surface side rise.In partial oxidation portion 12 although caused clinker is the shape of melting
State, but the clinker S of a part adheres to after the inner peripheral surface in partial oxidation portion 12 is cooled, and other parts, which are then fallen on, is located at part oxygen
The lower section D2 in change portion 12 slag notch 24 is simultaneously flowed out in preheating part 15 and is recovered.
In addition, the clinker S adhered on the inner peripheral surface in partial oxidation portion 12 is thicker, effect of heat insulation caused by clinker S is bigger, no
It is only capable of protecting part oxidation section 12 from the influence of high fever, moreover it is possible to reduce the water from partial oxidation portion 12 into cooling wall pipeline 22
Deng the heat (hereinafter referred to as " heat loss ") of conduction.
Here, heat loss is illustrated with Fig. 5.When by diameter than for 1/3 when heat loss amount be set to 1 (benchmark) and incite somebody to action
When the ratio of itself and the heat loss amount of other conditions are set to heat loss ratio, diameter than value more than 1/3 when heat loss ratio (L1) it is anxious
Drastic change is big.Because the axis C1 and the inner peripheral surface in partial oxidation portion 12 of burner nozzle 17 distance shorten.That is, from burner nozzle 17
The fluid of injection becomes easily towards inner peripheral surface and not towards the central part in partial oxidation portion 12.Therefore, it is attached to partial oxidation
Clinker on the inner peripheral surface in portion 12 becomes easily to peel off.In addition, when diameter ratio is less than 1/10, the inside in partial oxidation portion 12
The diameter of rotating flow drastically diminishes, therefore can not ensure the necessary reaction time, and reactivity ratio (L2) strongly reduces.It is referred to herein
Reactivity than refer to by diameter than for 1/3 when reactivity be set to 1 (benchmark) when its ratio with the reactivity of other conditions.
Also, as shown in fig. 6, when above-mentioned mean flow rate Va value is more than 50 (m/s), clinker becomes to hold as described above
Easily peel off, heat loss is than drastically becoming big.In addition, when mean flow rate Va is less than 10 (m/s), from coal supply arrangement 3 via burner
The air-flow transmission of coal of the portion 17 into coal gasifier 4 becomes unstable or becomes unable to carry out because of blocking, to partial oxidation
The coal quantity delivered in portion 12 can fluctuate.
Also, as shown in figure 1, supplied from the upper direction heat recovery equipment 5 of coal gasifier 4 along with coal tar with hydrogen and
Forming gas of the CO gas as the high temperature of principal component.
In heat recovery equipment 5, by make from coal gasifier 4 transmit the progress heat exchange of the forming gas and the boiler water that come come
Manufacture vapor.The vapor be conducted to above-mentioned coal crush and the grade of drying equipment 2 for coal drying the purpose of.
The forming gas being cooled in heat recovery equipment 5 is supplied to coal tar reclaimer 6 from heat recovery equipment 5, in coal tar
Recovery is included in the coal tar in forming gas in reclaimer 6.Here, the coal tar after recovery can also be used as fuel etc. to be used for outer
Portion is utilized, and the coal tar can also be made to recycle and be gasified in coal gasifier 4.
Transformationreation equipment 7 is supplied to by the forming gas after coal tar reclaimer 6.Also, in order to by forming gas
Hydrogen brings up to certain value relative to the ratio of CO gas, and vapor is supplied into transformationreation equipment 7, makes its hair
The raw transformationreation for having used catalyst as shown in following chemical equations (4).Pass through the transformationreation, CO gas
It is consumed, replaces and produce hydrogen.
CO+H2O→CO2+H2 (4)
The forming gas after composition is have adjusted in transformationreation equipment 7 and is supplied to gas refinishing equipment 8, reclaims forming gas
In contained carbon dioxide, include the gas of sulphur as composition etc..
Product forming gas after being refined in gas refinishing equipment 8 is supplied to chemical synthesis equipment etc., manufacture methane, methanol
And ammonia etc..
It is as discussed above, in the coal gasifier 4 of present embodiment, by burner nozzle 17 to cylindrical shape it is anti-
Supply coal and oxidant in container 12 are answered, the flowing of the central axis C2 rotations around reaction vessel 12 can be produced.Therefore, instead
Answer the flowing of the fluid near the inner peripheral surface of container 12 stable regardless of whether the position of circumferencial direction how, can make to be attached to reaction
On the inner peripheral surface of container 12 because of coal gasification and caused by the thickness of clinker that melts it is generally uniform.
In addition, burner nozzle 17 with the axis C1 of itself and plane-parallel or more towards the front end of burner nozzle more under
Square D2 mode configures.According to this composition, the combustion that gasification can be made to expand and rise on the inner edge of partial oxidation portion 12 rotation side
The coal of burning is before heat recovery equipment 5 is moved to from burner nozzle 17 first to horizontal or lower section D2 flowings.Therefore, it is possible to make from burning
High temperature director time of the coal particle that mouth 17 is blown near burner nozzle 17 is present, and then can increase the carbon (coal tar) in coal
The time flowed in partial oxidation portion 12, it is thus possible to make it fully vaporization in partial oxidation portion 12.
Also, because the central axis C2 of the surrounding portion oxidation section 12 of burner nozzle 17 is equally spaced configured, therefore it can make
Comprising the coal and the fluid of oxidant and the gas generated by coal gasification supplied from burner nozzle 17 in partial oxidation portion 12
Interior flowing is more stable.
In addition, burner nozzle 17 using imaginary diameter of a circle relative to the internal diameter of reaction vessel ratio as more than 1/10 and 1/3 with
Under mode configure.By making diameter ratio be less than 1/3, the speed of the fluid on the inner peripheral surface in partial oxidation portion 12 can be reduced
Gradient is spent, clinker of melting for suppressing to be attached on the inner peripheral surface in partial oxidation portion 12 etc. peels off from inner peripheral surface.Therefore, it is possible to anti-
The inner peripheral surface of stop point oxidation section 12 is exposed under high temperature and causes damage.And then by making diameter ratio be more than 1/10, energy
Head-on crash mutually occurs for coal and oxidant for enough preventing from supplying from burner nozzle 17 etc., positively produces surrounding portion oxidation section 12
Central axis C2 rotation flowing, so as to prevent reactivity than reduce.
Also, by making mean flow rate Va below, can suppress to be attached to the inner peripheral surface in partial oxidation portion 12 for 50 (m/s)
On clinker from inner peripheral surface peel off, so as to reduce the heat loss from partial oxidation portion 12 to exterior conductive.On the other hand, lead to
Crossing makes mean flow rate Va be more than 10 (m/s), can stably transmit coal using oxidant in burner nozzle 17.
In addition, by the way that the angle, θs of the axis C1 of burner nozzle 17 with respect to the horizontal plane are set into more than 0 ° and less than 10 °, energy
High temperature director time of the coal particle for enough making to be blown into from burner nozzle 17 near burner nozzle 17 is present, so that the gas of the carbon in coal
Change reaction to be promoted, it is possible to increase reactivity.
More than, embodiments of the present invention are described in detail referring to the drawings, but specific form is not limited to this
Embodiment, in addition to do not depart from composition change of scope of present subject matter etc..
For example, in the above-described embodiment, the shape of burner nozzle 17 is set to cylindric, but as long as being along defined axis
The shape of extension, can be flat cylindric or square tube shape etc..
In addition, in the above-described embodiment, even if burner nozzle 17 is not between central axis C2 of surrounding portion oxidation section 12 etc.
Configured every ground, the flowing of the fluid in partial oxidation portion 12 can also form the flowing of rotation, therefore burner nozzle 17 can not also
Equally spaced configured around central axis C2.
In addition, in above-mentioned coal gasifier, can also in the nearest top of the burner nozzle 17 in partial oxidation portion 12 and
Coal tar burner is configured on the second datum plane parallel with datum plane P1 in the same manner as burner nozzle 17.That is, coal tar burner can be with
During with from the D1 of top the axis of coal tar burner and diameter it is smaller than the internal diameter R1 in partial oxidation portion 12 and with central axis
Imaginary circle centered on C2 configures around the tangent mode of same direction.And then can also be with the axis and water of coal tar burner
Plane is parallel or more configures coal tar burner towards the front end of coal tar burner mode more downward.
In addition, on above-mentioned recycling, the mixing that can be uniformly mixed without using coal tar burner and by coal tar and coal
Thing is supplied to burner nozzle 17.
And then in the above-described embodiment, can possess pyrolysis portion on the top in partial oxidation portion 12, to from part oxygen
Change portion 12 using the hydrogen of high temperature and CO gas as the forming gas of principal component in be blown into coal, by above-mentioned forming gas
Heat is used to be pyrolyzed.
Embodiment
In the partial oxidation portion 12 of above-mentioned coal gasifier 4, the diameter of inner peripheral surface is set to 0.65 (m), internal height
1.0 (m) is set to, 4 burner nozzles 17 are equally spaced provided with partial oxidation portion 12.Also, made using the bituminous coal that ash content is 5%
Tested for coal.
The mean flow rate Va of burner nozzle 17 is set to 30 (m/s), by diameter ratio from 1/3 be changed into 1/5 operated after, can
Situation during than being set to 1/3 is known relative to diameter, when diameter is than being set to 1/5 from partial oxidation portion 12 into cooling wall pipeline 22
The above-mentioned heat loss of the conduction such as water reduces about 20%.
In addition, the diameter ratio in partial oxidation portion 12 is fixed as into 1/3, by the mean flow rate Va of burner nozzle 17 from 50 (m/s)
It is changed into after 30 (m/s) are operated, it is known that situation when relative to mean flow rate Va being 50 (m/s), mean flow rate Va is 30 (m/
Heat loss when s) reduces about 10%.
Also, mean flow rate Va is changed into 30 (m/s) from 50 (m/s) while diameter ratio is changed into 1/5 from 1/3 to carry out
After operating, heat loss reduces about 20%.
In addition, in the coal gasifier 4 of the shape of above-described embodiment, diameter ratio is set to 1/4, mean flow rate Va and is set to 10
(m/s) after and ash content is operated for 1% coal gasification, it is known that the clinker being attached on the inner peripheral surface in partial oxidation portion 12
Thickness is able to maintain that certain thickness.
Wherein, it is known that for above-mentioned heat loss, the situation for being 5% with ash content when ash content is more than 3% is identical, and ash content
For 5% situation about 30% is reduced than the situation that ash content is 1%.
4 coal gasifiers
12 partial oxidation portions (reaction vessel)
17a~17h burner nozzles
C1 axis
C2 central axis
E imaginary circles
P1 datum planes
θ angles
Claims (2)
1. a kind of manufacture method of forming gas, it is using coal gasifier, by making coal that part oxygen occur in reaction vessel
Change reaction and gasify to manufacture the method at least using hydrogen and CO gas as the forming gas of principal component, its feature exists
In,
The coal gasifier possesses：
The reaction vessel, it is formed as the cylindrical shape extended upward；
Outlet, it is arranged on the upper end side of the reaction vessel；With
The burner nozzle of multiple tubulars, it supplies coal and oxygen and vapor as oxidant into the reaction vessel, described
Coal is supplied by the 1st pipeline, and the oxidant is supplied by the 2nd pipeline different from the 1st pipeline,
The multiple burner nozzle is on the datum plane with plane-parallel positioned at the lower section of the outlet along the reaction
The circumferencial direction of the inner peripheral surface of container is set at spaced intervals,
The axis of each burner nozzle and the central axis with the reaction vessel during with from the top of the reaction vessel
Centered on and the diameter imaginary circle smaller than the internal diameter of reaction vessel described each burn is configured around the tangent mode of same direction
Mouth,
The imaginary diameter of a circle is set to more than 1/10 and less than 1/3 relative to the ratio of the internal diameter of the reaction vessel,
The burner nozzle is with the axis of the burner nozzle and plane-parallel or more towards the front end of the burner nozzle more direction
The mode of lower section configures, and the angle of the axis with respect to the horizontal plane is set to more than 0 ° and less than 10 °,
Methods described possesses is supplied respectively to the coal and institute into the reaction vessel by the burner nozzle in the following manner
The process for stating oxidant,
The mode is：When will be supplied from the coal from the burner nozzle to the reaction vessel, the quality of the oxidant
Flow is set to m1, m2, when the coal, the flow velocity of the oxidant in the burner nozzle are set into V1, V2, is obtained by (1) formula
Mean flow rate Va be set to more than 10m/s and below 50m/s,
Va=(m1 × V1+m2 × V2)/(m1+m2) (1)
Wherein, m1 and m2 unit is kg/s, and V1, V2 and Va unit are m/s,
Also, when being supplied respectively to the coal and the oxidant into the reaction vessel by the burner nozzle, the oxygen
The oxygen in agent supplies in the range of using the weight ratio meter with the coal as 0.7~0.9, the institute in the oxidant
Vapor is stated to supply in the range of using the weight ratio meter with the coal as 0.05~0.3.
2. the manufacture method of forming gas as claimed in claim 1, wherein, the burner nozzle is surrounded in the reaction vessel
Mandrel line equally spaced configures.
Applications Claiming Priority (3)
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| JP2010095496 | 2010-04-16 | ||
| JP2010-095496 | 2010-04-16 | ||
| CN2011800191978A CN102892870A (en) | 2010-04-16 | 2011-04-11 | Coal gasification furnace |
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| CN2011800191978A Division CN102892870A (en) | 2010-04-16 | 2011-04-11 | Coal gasification furnace |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| CN101558133A (en) * | 2005-06-28 | 2009-10-14 | 社区电力公司 | Method and apparatus for automated, modular, biomass power generation |
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| JPH0295687A (en) * | 1988-09-30 | 1990-04-06 | Toshiba Corp | Display device for cage position of elevator |
| JP3652720B2 (en) * | 1994-09-06 | 2005-05-25 | 三菱重工業株式会社 | Two-stage spouted bed coal gasifier |
| JPH08269466A (en) * | 1995-03-29 | 1996-10-15 | Mitsubishi Heavy Ind Ltd | Entrained bed coal gasifier |
| JP3504772B2 (en) * | 1995-04-25 | 2004-03-08 | 三菱重工業株式会社 | Spouted bed coal gasifier |
| AU730980B2 (en) * | 1996-05-20 | 2001-03-22 | Babcock-Hitachi Kabushiki Kaisha | Coal gasification apparatus and a coal gasification hybrid power generation system |
| JPH11269471A (en) * | 1998-03-23 | 1999-10-05 | Nippon Steel Corp | Coal rapid thermal decomposition oven and method for preventing char deposition |
| JP4435966B2 (en) * | 2000-11-21 | 2010-03-24 | 新日本製鐵株式会社 | Coal air bed type gasification method |
| JP4085239B2 (en) * | 2002-02-12 | 2008-05-14 | 株式会社日立製作所 | Gasification method and gasification apparatus |
| CN101392191B (en) * | 2008-10-15 | 2011-11-23 | 合肥工业大学 | Two stage type dry coal powder entrained flow gasifier |
| CN101508915B (en) * | 2009-03-17 | 2012-09-05 | 惠生工程（中国）有限公司 | Gasifying device for liquid fuel or solid fuel aqueous slurry |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| CN101558133A (en) * | 2005-06-28 | 2009-10-14 | 社区电力公司 | Method and apparatus for automated, modular, biomass power generation |
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| AU2011241999A1 (en) | 2012-12-06 |
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