CN102892870A - Coal gasification furnace - Google Patents
Coal gasification furnace Download PDFInfo
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- CN102892870A CN102892870A CN2011800191978A CN201180019197A CN102892870A CN 102892870 A CN102892870 A CN 102892870A CN 2011800191978 A CN2011800191978 A CN 2011800191978A CN 201180019197 A CN201180019197 A CN 201180019197A CN 102892870 A CN102892870 A CN 102892870A
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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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- 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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- 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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- 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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- 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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- 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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- 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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- 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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- 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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- 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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- 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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- 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]
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Abstract
Disclosed is a coal gasification furnace comprising: a reaction vessel (12) formed in a cylindrical shape extending upwards, equipped with an outlet at the upper end thereof; and a plurality of cylindrical burner units (17) disposed on a reference plane (P1) parallel to a horizontal plane and lower than the outlet, and in a circumferential direction with gaps left therebetween on an inside surface of the reaction vessel, which supply coal and an oxidising agent to the inside of the reaction vessel; and coal is burned inside the reaction vessel to produce at least hydrogen gas and carbon monoxide gas. When seen from above, the axes (C1) of the burners are oriented in the same direction as and touch an imaginary circle centred on a central axis with a diameter less than the inside diameter of the reaction vessel, where the axes are parallel to a horizontal plane or where the tips of the burner units are oriented downwards.
Description
Technical field
The present invention relates to oxygenants such as oxygen, water vapour gasification be produced the coal gasifier of inflammable gas.
The Japanese Patent Application 2010-095496 number opinion right of priority that the application filed an application in Japan based on April 16th, 2010, and here cite its content.
Background technology
In the past, as the vapourizing furnace (coal gasifier) of being produced inflammable gas by fine coal etc., for example known had a vapourizing furnace shown in the patent documentation 1.In this vapourizing furnace, in pressurized vessel (reaction vessel), overlook on the circumference in the plane that 4 roasting kiln burners (combustor burner) when observing are configured in regulation equidistantly.And, clip the central shaft of circumference and be configured in symmetrical locational 2 groups of roasting kiln burners and configure in mutual opposed mode.
The roasting kiln burner by be arranged on central part and be used for to start vapourizing furnace the light oil burner, air nozzle, coal tar nozzle, fuel coal nozzle, the secondary air nozzle of configuration consist of successively laterally by the inboard to be concentric circles ground with the light oil burner.
After air, coal tar (not gasification of coal residue or pyrolysis residue), fuel coal rotate in nozzle separately, lighted by the light oil burner and in pressurized vessel, spray.
The prior art document
Patent documentation
Patent documentation 1: No. 3595404 communique of Japanese Patent
Summary of the invention
The technical problem that invention will solve
But, in the vapourizing furnace shown in the above-mentioned patent documentation 1, there is following problem: when the gas that sprays rotational flow from each roasting kiln burner etc., because the roasting kiln burner is configured on the mutual opposed position, therefore the gas that ejects from the roasting kiln burner etc. are collision mutually, the flowing instability of the gas in the vapourizing furnace etc.And, the inner peripheral surface of vapourizing furnace is exposed under the hot environment because of the partial oxidation (hereinafter referred to as " gasification ") of coal, if on the inner peripheral surface of vapourizing furnace, stably do not adhere to certain thickness slag, then have following possibility: not only the thermosteresis change causes greatly performance to reduce, and this inner peripheral surface also can be subject to the impact of heat and produce damage.
And then, rise in vapourizing furnace by the meetings such as gas that gasification produces, but when the upwelling movable property of the gas in the vapourizing furnace etc. is given birth to when uneven, carbon in coal (coal tar) flows out from vapourizing furnace before the generating gasification reaction fully sometimes, and reactivity (carbon in the coal is to the transformation efficiency of gas reforming) is reduced.
The present invention puts in view of the above problems and finishes, and its purpose is to provide a kind of and coal is reacted in the reaction vessel of compactness fully and makes slag stably be attached to high efficiency coal gasifier on the inner peripheral surface of reaction vessel.
The means that are used for the technical solution problem
In order to solve the problems of the technologies described above, the present invention proposes following means.
Coal gasifier of the present invention possesses:
Reaction vessel, it forms the cylindric of upward extension and is provided with relief outlet in upper end side; With
The burner nozzle of tubular, its parallel with horizontal plane and be positioned at above-mentioned relief outlet below reference plane on the inner peripheral surface at described reactor compartment of terrain spaced apart in the circumferential direction arrange a plurality of, and in the above-mentioned reaction vessel for coal supply and oxygenant,
In described coal gasifier, by being gasified, above-mentioned coal makes at least hydrogen and CO (carbon monoxide converter) gas in above-mentioned reaction vessel,
It is characterized in that, each above-mentioned burner nozzle axis and diameter of self when observing from the top and imaginary circle by above-mentioned central axis centered by less than the internal diameter of above-mentioned reaction vessel is tangent and self axis is parallel with horizontal plane or more more configure towards the mode of below towards the front end of above-mentioned burner nozzle around same direction.
That is, in the present invention, be characterised in that by make the coal coal gasifier of making at least hydrogen and CO (carbon monoxide converter) gas that gasifies in reaction vessel, it has:
Reaction vessel, it forms extend upward cylindric;
Relief outlet, it is arranged on the upper end side of above-mentioned reaction vessel; With
The burner nozzle of a plurality of tubulars, it supplies coal supply and oxygenant in above-mentioned reaction vessel,
Above-mentioned a plurality of burner nozzle be positioned at above-mentioned relief outlet below the reference plane parallel with horizontal plane on arrange towards the circumferential direction devices spaced apart ground of the inner peripheral surface of above-mentioned reaction vessel,
When observing from the top of above-mentioned reaction vessel the axis of above-mentioned each burner nozzle with centered by the central axis of above-mentioned reaction vessel and the diameter imaginary circle less than the internal diameter of reaction vessel configure above-mentioned each burner nozzle around the tangent mode of same direction,
Above-mentioned burner nozzle is parallel with horizontal plane or more more configure towards the mode of below towards the front end of above-mentioned burner nozzle with the axis of above-mentioned burner nozzle.
According to the present invention, when burner nozzle in the reaction vessel cylindraceous during for coal supply and oxygenant, can produce flowing around the fluid of the central axis rotation of reaction vessel.Therefore, near the optional position that is flowing in circumferential direction of the fluid the inner peripheral surface of reaction vessel is all stable, can make the thickness of slag of the melting that produces because of gasification on the inner peripheral surface that is attached to reaction vessel roughly even.
In addition, burner nozzle is parallel with horizontal plane or more more configure towards the mode of below towards the front end of burner nozzle with the axis of self.By make gasification expand and the coal that rises on reaction vessel inner edge rotation limit from burner nozzle first to level or below flow, thereby can increase the time that coal flows in reaction vessel, make its discharge from relief outlet before fully gasification in reaction vessel.
In addition, in above-mentioned coal gasifier, above-mentioned burner nozzle more preferably equally spaced configures around the central axis of above-mentioned reaction vessel.
According to the present invention, can make the coal supplied with from burner nozzle comprising in the reaction vessel and oxygenant and the fluid of the gas that produces because of burning of coal flow more stable.
In addition, in above-mentioned coal gasifier, above-mentioned imaginary circular diameter more preferably is set as more than 1/10 with respect to the ratio of the internal diameter of above-mentioned reaction vessel and below 1/3.
According to the present invention, by imaginary circular diameter is made as below 1/3 with respect to the ratio of the internal diameter of reaction vessel (below be also referred to as " diameter ratio "), can reduce the velocity slope of the fluid on the inner peripheral surface of reaction vessel, the slag that suppresses to be attached on the inner peripheral surface of reaction vessel peels off from inner peripheral surface.The inner peripheral surface that therefore, can prevent reaction vessel is exposed to that the increase because of thermosteresis causes performance to reduce or the inner peripheral surface damage under the high temperature.
In addition, by the diameter ratio is made as more than 1/10, can prevent that the coal supplied with from burner nozzle and oxygenant etc. from head-on crash occuring mutually, positively produce around the flowing of the central axis rotation of reaction vessel, make the gasification reaction time elongated, improve reactivity.
In addition, in above-mentioned coal gasifier, when will be from each above-mentioned coal of supplying with in the above-mentioned reaction vessel of above-mentioned burner nozzle, the mass rate of above-mentioned oxygenant be made as m1 (kg/s), m2 (kg/s), when the flow velocity of the above-mentioned coal in each above-mentioned burner nozzle, above-mentioned oxygenant was made as V1 (m/s), V2 (m/s), it is above and below 50 (m/s) that the mean flow rate Va (m/s) that is obtained by (1) formula more preferably is set as 10 (m/s).
Va=(m1×V1+m2×V2)/(m1+m2)(1)
According to the present invention, by mean flow rate Va is made as below 50 (m/s), the slag that can suppress to be attached on the inner peripheral surface of reaction vessel peels off from inner peripheral surface, thereby can reduce the thermosteresis from reaction vessel to exterior conductive.In addition, by mean flow rate Va being made as more than 10 (m/s), can utilize oxygenant stably to transmit coal at burner nozzle.
In addition, in above-mentioned coal gasifier, the axis of each above-mentioned burner nozzle angle with respect to the horizontal plane more preferably is set as more than 0 ° and below 10 °.
According to the present invention, by being made as this angle more than 0 ° and below 10 °, can making near the high temperature director time of coal particle burner nozzle that burner nozzle is blown into to exist, thereby the gasification reaction of coal tar is promoted, can improve reactivity.
In addition, in above-mentioned coal gasifier, more preferably the above-mentioned burner nozzle in above-mentioned reaction vessel nearest above and with parallel plane the second reference plane of said reference on above-mentioned burner nozzle the coal tar burner is set similarly.
According to the present invention, the coal tar that unreacted is recovered by the coal tar burner that utilizes reaction vessel recycles in coal gasifier and makes its generating gasification reaction, and can make the Carbon gasification reactivity in the coal is more than 99%.
The invention effect
According to coal gasifier of the present invention, coal is reacted in the reaction vessel of compactness fully, and slag stably is attached on the inner peripheral surface of reaction vessel.
Description of drawings
Fig. 1 is the block diagram of synthesis gas from coal gasification system manufacturing system that has used the coal gasifier of embodiment of the present invention.
Fig. 2 is the longitudinal diagram of major portion of the coal gasifier of embodiment of the present invention.
Fig. 3 is the top plan view along the line of cut A-A among Fig. 2.
Fig. 4 is the figure of the velocity flow profile of the reference plane in the presentation graphs 3.
Fig. 5 be in the partial oxidation section of coal gasifier of expression embodiment of the present invention thermosteresis than and reactivity than and diameter than between the figure of relation.
Fig. 6 be in the coal gasifier of expression embodiment of the present invention thermosteresis than and the mean flow rate of coal and oxygenant between the figure of relation.
Embodiment
Below, the limit describes referring to figs. 1 through the embodiment of Fig. 6 limit to coal gasifier of the present invention.Coal gasifier be assembled into to come in the part of gasification system with and by making coal make at least the device of hydrogen and CO (carbon monoxide converter) gas in internal-combustion.
As shown in Figure 1, synthesis gas from coal gasification system manufacturing system 1 is that coal is made with hydrogen and the CO (carbon monoxide converter) gas suite of equipment as the synthesis gas of principal constituent as raw material.By this product synthesis gas is supplied with as the raw material of chemosynthesis equipment etc., finally can make methane, methyl alcohol and ammonia etc.
Synthesis gas from coal gasification system manufacturing system 1 possesses coal gasifier 4, heat recovery equipment 5, coal tar recovery system 6, transformationreation equipment 7, gas refinishing equipment 8 and the air separation equipment 9 of coal pulverizer and drying plant 2, coal supply arrangement 3, present embodiment.
Usually, the external diameter of coal is inhomogeneous, sometimes contains moisture more than desired value according to its kind.For this reason, at first in coal pulverizer and drying plant 2, coal is pulverized, take form below 200 orders as about 75%, the fine coal of median size as about 30～60 (the μ m), then carry out drying, in the moisture content that reaches regulation, preferably reach below 10% with the total moisture amount, then be supplied to coal supply arrangement 3.In addition, till the coal gasifier 4, do not change in order to make the amount of moisture in the dried coal after coal pulverizer and drying plant 2, coal is mobile in airtight space.
Then, for interior for coal supplies to coal gasifier 4, coal supply arrangement 3 is interior utilize carrier gas etc. to boost to the pressure of regulation after, transmit coal to coal gasifier 4 weight feed predetermined weights by air-flow.The running pressure of coal gasifier is not particularly limited, but the viewpoint that the raising of the reaction efficiency that brings from the vapourizing furnace densification, installation cost and charges for water and electricity reduce, and is preferably 2MPaG above and below the 5MPaG.
On the other hand, air separation equipment 9 makes air compressing its liquefaction and utilizes and separate dry oxygen and nitrogen etc. the air of difference after becoming liquid of boiling point.Supplied with to coal gasifier 4 with the regulation flow by air separation equipment 9 isolated oxygen.
As shown in Figure 2, coal gasifier 4 up D1 has partial oxidation section (reaction vessel) 12 at least, and D2 is provided with preheating part 15 below partial oxidation section 12.Partial oxidation section 12 and preheating part 15 are communicated with at above-below direction D.
As shown in Figures 2 and 3, partial oxidation section 12 is by using stable on heating refractory body etc. to form cylindric that D along the vertical direction extends, on the inner peripheral surface of partial oxidation section 12, be provided with form 8 burner nozzle 17a～17h cylindraceous of extending along axis C1 (below, when not having special difference earth's surface to show these burner nozzles 17a～17h, they are referred to as " burner nozzle 17 ").
In addition, to the not restriction of the quantity that is arranged on the burner nozzle 17 in the partial oxidation section 12, so long as what can more than 2.Wherein, preferably along with the size of partial oxidation section 12 become greatly with 4,6,8 ... such mode is set to even number with accelerating, even but odd number is also fully no problem.
8 burner nozzles 17 are arranged on the reference plane P1 parallel with horizontal plane, and equally spaced configure around the central axis C 2 of partial oxidation section 12.
About burner nozzle 17, as shown in Figure 3, the axis C1 of burner nozzle 17 configures around the tangent mode of same direction F1 than the internal diameter R1 of partial oxidation section 12 imaginary circle E less and centered by central axis C 2 with diameter when observing from top D1.Here, refer to around same direction F1 is tangent, when line that the axis C1 with each burner nozzle 17 is considered as extending from the front end of burner nozzle 17, axis C1 is tangent around direction F1 with respect to imaginary circle E.In addition, can be that the tangent mode of direction F2 configures with imaginary circle E around the direction opposite with direction F1 with the axis C1 of each burner nozzle 17 also.
And, be diameter than reaching more than 1/10 and 1/3 following mode is set with imaginary circular diameter R2 with respect to the ratio (the internal diameter R1 of imaginary circular diameter R2/ reaction vessel) of the internal diameter R1 of partial oxidation section 12.Diameter is than more preferably more than 1/5 and below 3/10.
And then, as shown in Figure 2, reach more than 0 ° and the mode below 10 ° is set with the axis C1 angle θ with respect to the horizontal plane of burner nozzle 17.
That is, the front end of burner nozzle 17 preferably tilts to the below of partial oxidation section 12 and with respect to the horizontal plane is more than 0 ° and below 10 °, more preferably more than 0 ° and below 2 °.
Supplied to each burner nozzle 17 by the flow of coal supply unit 20 with regulation by the coal of pulverizing and dried micro mist shape in coal pulverizer and the drying plant 2.By air separation equipment 9 isolated oxygen and the water vapour supplied with by heat recovery equipment 5 as described later by oxygenant supply unit 21 with the flow of regulation for to each burner nozzle 17.
More specifically, to be made as m1 (kg/s), m2 (kg/s) for the coal to partial oxidation section 12, the mass rate of oxygenant (oxygen and water vapour) from burner nozzle 17, the coal in the burner nozzle 17, the flow velocity of oxygenant will be made as V1 (m/s), V2 (m/s).At this moment, reach the mode that 10 (m/s) are above and 50 (m/s) are following with the mean flow rate Va (m/s) that is obtained by following (2) formula, regulate the flow of coal and oxygenant by coal supply unit 20 and oxygenant 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 that penetrates from the raw material jet orifice of burner nozzle 17.
Wherein, the oxygen in the oxygenant count 0.7～0.9 scope with the weight ratio (oxygen/coal) of oxygen and coal in, water vapour counting in 0.05～0.3 the scope, suitably setting according to coal kind and operating plan temperature with the weight ratio (water vapour/coal) of water vapour and coal.In addition, the flow velocity V1 (m/s) of the oxygenant in the burner nozzle 17 is made as the flow velocity under oxygen and the mixed state of water vapour.About the difference of coal kind, can form etc. with coal industrial analysis value and ultimate analysis value, ash and represent.
In addition, mean flow rate Va is more preferably more than 10 (m/s) and below 30 (m/s).
On the periphery of partial oxidation section 12, be equipped with the cooling stave pipeline 22 for cooling segment oxidation section 12, be connected with for the pump 23 to its inner inflow water or saturation water (feedwater) at cooling stave pipeline 22.Can also partial oxidation section 12 can be heated as boiler at cooling stave pipeline 22 internal recycle at these cooling stave pipeline 22 interior mobile water or saturation water, form behind the water vapour of high temperature as vapor recovery and utilization.
Pulverized and boost after coal and oxygenant with mean flow rate Va from above-mentioned burner nozzle 17 for to partial oxidation section 12.8 burner nozzles 17 are because as shown in Figure 3 configuration, and the coal of therefore supplying with from burner nozzle 17 and oxygenant at first spray downwards or in the mode that same level flows around the central axis C 2 rotation limits of partial oxidation section 12 with the limit as shown in Figure 2.Become high temperature and high pressure (for example temperature is more than 1200 ℃ and below 1800 ℃, pressure be more than the 2MPa) in the partial oxidation section 12.Under this environment, coal becomes high temperature and pyrolysis occurs, coal tar separates with the volatile gases that comprises tar and water vapour etc., coal generating gasification meanwhile, thus CO (carbon monoxide converter) gas, carbon dioxide and hydrogen and slag (ash content) based on the high temperature of following chemical equation (1)～(3) produced.
2C+O
2→2CO (1)
C+O
2→CO
2(2)
C+H
2O→CO+H
2(3)
The velocity flow profile of hydrogen and CO (carbon monoxide converter) gas etc. is shown in Fig. 4 in each position in the partial oxidation section 12 at this moment.Fig. 4 is the figure of flow velocity v that is illustrated in the upper position from central axis C2 to the r direction of reference plane P2 of the central axis C that comprises partial oxidation section 12 2 shown in Figure 3.Here, reference plane P2 is the face vertical with respect to the reference plane P1 parallel with horizontal plane.In partial oxidation section 12, (r direction) limit rises around same direction (for example direction F1) rotation limit the fluids such as hydrogen and CO (carbon monoxide converter) gas from central axis C2 to radial direction.Fig. 4 shows the variation (distribution) of flow velocity v of the fluid of r direction on position of certain height of this reference plane P2.Here, the position of certain height refers to along the optional position of the short transverse of partial oxidation section 12, as long as on burner nozzle 17a.In Fig. 4, transverse axis represents that the longitudinal axis represents flow velocity v with respect to the position of the r direction of central axis C 2.In addition, in fact the position of r direction is different with the direction of the position of r direction flow velocity v when minus side (among Fig. 3 be burner nozzle 17e side with respect to central axis C 2) when positive side (being burner nozzle 17a side with respect to central axis C 2 among Fig. 3), but Fig. 4 only shows the size of flow velocity v and do not consider its direction.In addition, Fig. 4 does not consider to be attached to the thickness of the aftermentioned slag on the inner peripheral surface of partial oxidation section 12.
In Fig. 4, represent to reach more than 1/5 with respect to the ratio of the internal diameter of partial oxidation section (reaction vessel) 12 and 3/10 following mode arranges burner nozzle 17 and is made as mean flow rate Va more than 10 (m/s) and the model of the flow velocity v of 30 (m/s) when following in partial oxidation section 12 with imaginary circular diameter with solid line.
In Fig. 4, shown in solid line, the position on the axis C1 of burner nozzle 17c be the position of r direction be near the position of R2/2, and the axis C1 of burner nozzle 17g on the position be near the position of position for-R2/2 of r direction, flow velocity v is maximum.And, the position that in the position of the inner peripheral surface of partial oxidation section 12 is the r direction be R1/2 the position, and be the position of-R1/2, flow velocity v is near 0, and the absolute value of the slope of a curve of flow velocity v (velocity slope) becomes less value.
When hydrogen and CO (carbon monoxide converter) gas etc. is assumed to be Newtonian fuid, the power (shearing force) that fluid attempts to peel off slag multiply by the value (μ (dv/dr)) that the coefficient of viscosity μ of fluid gets for the velocity slope of the flow velocity v of fluid, and therefore the shearing force of this moment is less as can be known.
Relative therewith, surpassed in the comparative example of 50 (m/s) at the mean flow rate Va that is obtained by (2) formula, as shown in phantom in Figure 4, flow velocity v is peaked invariant position, but the maximum value of flow velocity v increases.Therefore, the absolute value of the slope of a curve of flow velocity v increases, and the shearing force that acts on slag increases, and slag becomes and easily peels off.
In addition, formation with respect to the partial oxidation section 12 of the velocity flow profile that the fluid shown in the solid line is shown, leave and make diameter than having surpassed 1/3 the comparative example from the central axis C 2 of partial oxidation section 12 at the axis C1 that makes burner nozzle 17b, the velocity flow profile of fluid becomes the distribution shown in the two dot chain line among Fig. 4.Namely, under these circumstances, also owing to the position of the inner peripheral surface of partial oxidation section 12 be the position of r direction be R1/2 and-absolute value of the slope of a curve of the flow velocity v of the position of R1/2 increases increases the shearing force that acts on slag, so slag also becomes and easily peels off.
As shown in Figure 2, in the gas of partial oxidation section 12 interior generations and the equilateral outer side shifting of central axis C 2 rotation limit radius vector directions around partial oxidation section 12 of slag, thereby and become high temperature and expand and under the effect of buoyancy, be subject to power upwards and in the inner peripheral surface side rising of partial oxidation section 12.Although the slag in the 12 interior generations of partial oxidation section is the state of melting, but the slag S of a part is at the inner peripheral surface of partial oxidation section 12 postadhesion that is cooled, and other parts are then fallen the slag notch 24 of the below D2 that is located at partial oxidation section 12 and flowed out in the preheating part 15 and be recovered.
In addition; the slag S that adheres on the inner peripheral surface of partial oxidation section 12 is thicker; the effect of heat insulation that slag S produces is larger; can not only protect partial oxidation section 12 to avoid the impact of high heat, can also reduce from partial oxidation section 12 to the cooling stave pipeline heat (hereinafter referred to as " thermosteresis ") of the conduction such as water in 22.
Here, with Fig. 5 thermosteresis is described.When the heat loss amount of diameter when being 1/3 is made as 1 (benchmark) its ratio with the heat loss amount of other conditions is made as thermosteresis than the time, it is larger than (L1) rapid change that the value of diameter ratio surpasses 1/3 o'clock thermosteresis.This is because the distance of the inner peripheral surface of the axis C1 of burner nozzle 17 and partial oxidation section 12 shortens.That is the fluid that, penetrates from burner nozzle 17 becomes easily towards inner peripheral surface and not towards the central part of partial oxidation section 12.Therefore, being attached to slag on the inner peripheral surface of partial oxidation section 12 becomes and easily peels off.In addition, when the diameter ratio was lower than 1/10, the diameter of the rotating fluid of the inside of partial oxidation section 12 sharply diminished, and therefore can't guarantee the necessary reaction times, and reactivity sharply reduces than (L2).Here the ratio of said reactivity reactivity of itself and other condition when referring to that diameter is made as 1 (benchmark) than the reactivity that is at 1/3 o'clock.
And as shown in Figure 6, when the value of above-mentioned mean flow rate Va surpassed 50 (m/s), slag became and easily peels off as described above, and thermosteresis is than sharply becoming large.In addition, when mean flow rate Va is lower than 10 (m/s), transmits via the air-flow of the coal of burner nozzle 17 in the coal gasifier 4 from coal supply arrangement 3 and to become unstable or can not carry out because obstruction becomes, can fluctuate to the coal feed rate of partial oxidation section 12.
And, as shown in Figure 1, from the top of coal gasifier 4 to heat recovery equipment 5 supply be accompanied by coal tar with hydrogen and the CO (carbon monoxide converter) gas synthesis gas as the high temperature of principal constituent.
In heat recovery equipment 5, make water vapour by making the synthesis gas that sends from coal gasifier 4 and feedwater carry out heat exchange.This water vapour is conducted to above-mentioned coal pulverizer and drying plant 2 etc. to be used for the purposes such as drying of coal.
The synthesis gas that is cooled in heat recovery equipment 5 for to coal tar recovery system 6, reclaims the coal tar that is included in the synthesis gas from heat recovery equipment 5 in coal tar recovery system 6.Here, the coal tar after the recovery also can be used as fuel etc. and is used for outside the utilization, this coal tar is recycled in coal gasifier 4 and gasifies.
Supply to transformationreation equipment 7 by the synthesis gas behind the coal tar recovery system 6.And, for hydrogen in the synthesis gas is brought up to certain value with respect to the ratio of CO (carbon monoxide converter) gas, in transformationreation equipment 7, supply with water vapour, made its occur shown in following chemical equation (4) use the transformationreation of catalyzer.By this transformationreation, CO (carbon monoxide converter) gas is consumed, and generation hydrogen replaces.
CO+H
2O→CO
2+H
2(4)
In transformationreation equipment 7, regulated synthesis gas behind the composition for to gas refinishing equipment 8, reclaimed carbon dioxide contained in the synthesis gas, comprise sulphur as the gas of composition etc.
Product synthesis gas after refining in gas refinishing equipment 8 is made methane, methyl alcohol and ammonia etc. for to chemosynthesis equipment etc.
As discussed above, in the coal gasifier 4 of present embodiment,, can produce around flowing that the central axis C 2 of reaction vessel 12 is rotated to reaction vessel 12 interior coal supply and the oxygenants of supplying cylindraceous by burner nozzle 17.Therefore, near the flowing stable of fluid the inner peripheral surface of reaction vessel 12 and regardless of the position of circumferential direction can make the thickness of slag of the melting that produces because of gasification on the inner peripheral surface that is attached to reaction vessel 12 roughly even.
In addition, burner nozzle 17 is parallel with horizontal plane or more more configure towards the mode of below D2 towards the front end of burner nozzle with the axis C1 of self.Consist of according to this, can make gasification expand and the coal of the burning that rises on partial oxidation section 12 inner edges rotation limit moving to heat recovery equipment 5 before from burner nozzle 17 first to level or below D2 flow.Therefore, can make near the high temperature director time of coal particle burner nozzle 17 that burner nozzle 17 is blown into and exist, and then can increase the time that the carbon (coal tar) in the coal flows in partial oxidation section 12, thereby can make its fully gasification in partial oxidation section 12.
And, because burner nozzle 17 equally spaced configure around the central axis C 2 of partial oxidation section 12, mobile more stable in partial oxidation section 12 of the fluid that therefore can make the gas that comprises the coal supplied with from burner nozzle 17 and oxygenant and generate because of coal gasification.
In addition, burner nozzle 17 configures as the mode more than 1/10 and below 1/3 with respect to the ratio of the internal diameter of reaction vessel take imaginary circular diameter.Be below 1/3 by making the diameter ratio, can reduce the velocity slope of the fluid on the inner peripheral surface of partial oxidation section 12, the slag etc. that suppresses to be attached to the melting on the inner peripheral surface of partial oxidation section 12 peels off from inner peripheral surface.The inner peripheral surface that therefore, can prevent partial oxidation section 12 is exposed under the high temperature and causes damage.And then, be more than 1/10 by making the diameter ratio, can prevent that the coal supplied with from burner nozzle 17 and oxygenant etc. from head-on crash occuring mutually, positively produce around the flowing of central axis C 2 rotations of partial oxidation section 12, thereby can prevent reactivity than reducing.
And, be below 50 (m/s) by making mean flow rate Va, the slag that can suppress to be attached on the inner peripheral surface of partial oxidation section 12 peels off from inner peripheral surface, thereby can reduce the thermosteresis from partial oxidation section 12 to exterior conductive.On the other hand, be more than 10 (m/s) by making mean flow rate Va, can in burner nozzle 17, utilize oxygenant stably to transmit coal.
In addition, be made as more than 0 ° and below 10 ° by the axis C1 angle θ with respect to the horizontal plane with burner nozzle 17, can make near the high temperature director time of coal particle burner nozzle 17 that burner nozzle 17 is blown into to exist, thereby the Carbon gasification reaction in the coal is promoted, can improve reactivity.
Above, with reference to accompanying drawing embodiments of the present invention are described in detail, but concrete formation is not limited to this embodiment, also comprise the formation change of the scope that does not break away from purport of the present invention etc.
For example, in the above-described embodiment, the shape of burner nozzle 17 being made as cylindric, but so long as get final product along the shape of the Axis Extension of regulation, can be flat cylindric or square tube shape etc.
In addition, in the above-described embodiment, even burner nozzle 17 does not equally spaced configure around the central axis C 2 of partial oxidation section 12, flowing of the fluid in the partial oxidation section 12 also can form flowing of rotation, so burner nozzle 17 can equally spaced not configure around central axis C 2 yet.
In addition, in above-mentioned coal gasifier, similarly configure the coal tar burner with burner nozzle 17 above burner nozzle 17 that can also be in partial oxidation section 12 nearest and on second reference plane parallel with reference plane P1.That is, the coal tar burner can be when observing from top D1 axis and the diameter of coal tar burner less and configure around the tangent mode of same direction with imaginary circle centered by central axis C 2 than the internal diameter R1 of partial oxidation section 12.And then, can also be with the axis of coal tar burner parallel with horizontal plane or more towards the front end of coal tar burner more the mode towards the below configure the coal tar burner.
In addition, about above-mentioned recycling, can not use the coal tar burner and mixture that coal tar and coal are evenly mixed for to burner nozzle 17.
And then, in the above-described embodiment, top in partial oxidation section 12 can possess pyrolysis section, is blown into coal to hydrogen and CO (carbon monoxide converter) gas take high temperature from partial oxidation section 12 in the synthesis gas of principal constituent, and the heat of above-mentioned synthesis gas is used for pyrolysis.
Embodiment
In the partial oxidation section 12 of above-mentioned coal gasifier 4, with the diameter of inner peripheral surface be made as 0.65 (m), inner height is made as 1.0 (m), equally spaced is provided with 4 burner nozzles 17 in partial oxidation section 12.And using ash content is that 5% bituminous coal is tested as coal.
The mean flow rate Va of burner nozzle 17 is made as 30 (m/s), with diameter than from 1/3 become 1/5 carried out the running after, as can be known with respect to diameter than the situation that is made as at 1/3 o'clock, diameter reduces approximately 20% than the above-mentioned thermosteresis that is made as the conduction such as water in 22 from partial oxidation section 12 to the cooling stave pipeline in 1/5 o'clock.
In addition, the diameter ratio of partial oxidation section 12 is fixed as 1/3, after the mean flow rate Va of burner nozzle 17 become 30 (m/s) and turn round from 50 (m/s), situation when being 50 (m/s) with respect to mean flow rate Va as can be known, the thermosteresis when mean flow rate Va is 30 (m/s) reduce approximately 10%.
And after when diameter is become 1/5 than from 1/3 mean flow rate Va being become 30 (m/s) from 50 (m/s) and turning round, thermosteresis reduces approximately 20%.
In addition, in the coal gasifier 4 of the shape of above-described embodiment, with the diameter ratio be made as 1/4, mean flow rate Va is made as 10 (m/s) and be after 1% gasification turns round with ash content, the slag thickness that is attached to as can be known on the inner peripheral surface of partial oxidation section 12 can be kept certain thickness.
Wherein, as can be known for above-mentioned thermosteresis, be 3% to be that 5% situation is identical with ash content when above when ash content, be that 1% situation reduces approximately 30% and ash content is 5% situation than ash content.
4 coal gasifiers
12 partial oxidation sections (reaction vessel)
17a～17h burner nozzle
The C1 axis
The C2 central axis
The E imaginary circle
The P1 reference plane
The θ angle
Claims (5)
1. coal gasifier, it makes hydrogen and CO (carbon monoxide converter) gas at least by coal is gasified in reaction vessel, it is characterized in that having:
Reaction vessel, it forms extend upward cylindric;
Relief outlet, it is arranged on the upper end side of described reaction vessel; With
The burner nozzle of a plurality of tubulars, it supplies coal supply and oxygenant in described reaction vessel,
Described a plurality of burner nozzle be positioned at described relief outlet below the reference plane parallel with horizontal plane on arrange along the circumferential direction devices spaced apart ground of the inner peripheral surface of described reaction vessel,
When observing from the top of described reaction vessel the axis of described each burner nozzle with centered by the central axis of described reaction vessel and the diameter imaginary circle less than the internal diameter of reaction vessel configure described each burner nozzle around the tangent mode of same direction,
Described burner nozzle is parallel with horizontal plane or more more configure towards the mode of below towards the front end of described burner nozzle with the axis of described burner nozzle.
2. coal gasifier as claimed in claim 1, wherein, described burner nozzle equally spaced configures around the central axis of described reaction vessel.
3. coal gasifier as claimed in claim 1 or 2, wherein, described imaginary circular diameter is set to more than 1/10 with respect to the ratio of the internal diameter of described reaction vessel and below 1/3.
4. such as each described coal gasifier in the claims 1 to 3, wherein, when will be from each described coal of supplying with in the described reaction vessel of described burner nozzle, the mass rate of described oxygenant be made as m1, m2, when the flow velocity of the described coal in each described burner nozzle, described oxygenant is made as V1, V2, the mean flow rate Va that is obtained by (1) formula is set to more than the 10m/s and below the 50m/s
Va=(m1×V1+m2×V2)/(m1+m2)(1)
Wherein, the unit of m1 and m2 is kg/s, and the unit of V1, V2 and Va is m/s.
5. such as each described coal gasifier in the claim 1 to 4, wherein, the axis of each described burner nozzle angle with respect to the horizontal plane is set to more than 0 ° and below 10 °.
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| PCT/JP2011/059020 WO2011129302A1 (en) | 2010-04-16 | 2011-04-11 | Coal gasification furnace |
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| CN108998097A (en) * | 2018-08-28 | 2018-12-14 | 朋仁锋 | A kind of coal gasification method |
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| JPWO2011129302A1 (en) | 2013-07-18 |
| CN104479748B (en) | 2018-01-05 |
| WO2011129302A1 (en) | 2011-10-20 |
| CN104479748A (en) | 2015-04-01 |
| JP5552157B2 (en) | 2014-07-16 |
| AU2011241999B2 (en) | 2013-12-19 |
| AU2011241999A1 (en) | 2012-12-06 |
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