CN102884162A - Operational method for coal gasification reaction furnace and coal gasification reaction furnace - Google Patents
Operational method for coal gasification reaction furnace and coal gasification reaction furnace Download PDFInfo
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- CN102884162A CN102884162A CN2011800187173A CN201180018717A CN102884162A CN 102884162 A CN102884162 A CN 102884162A CN 2011800187173 A CN2011800187173 A CN 2011800187173A CN 201180018717 A CN201180018717 A CN 201180018717A CN 102884162 A CN102884162 A CN 102884162A
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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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- 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
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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
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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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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- 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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- 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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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- 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
- 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 an operational method for a coal gasification reaction furnace comprising a lower reaction vessel and an upper reaction vessel communicating with each other, which includes the following steps: a step wherein carbon raw material, oxygen gas and water vapour are supplied inside the lower reaction vessel; a step wherein coal is supplied using a coal nozzle, and water vapour is supplied using a water nozzle, inside the upper reaction vessel; a step wherein the coal in the upper reaction chamber is reacted at a temperature of 950 DEG C or higher by the high-temperature gas produced in the lower reaction vessel and a synthesis gas containing at least hydrogen gas and carbon monoxide gas is produced; and a step wherein the mass flow rate of the coal supplied by the coal nozzle and/or the mass flow rate of the water vapour supplied by the water vapour nozzle are adjusted such that the ratio of mass flow rate (Qs) of the water vapour content of the synthesis gas and mass flow rate (Qc) of the carbon supplied to the upper reaction vessel, Qs/Qc, is 1.0-1.5.
Description
Technical field
The present invention relates to oxygenants such as oxygen or water vapour gasification be produced method of operation and the coal gasification reaction stove of the coal gasification reaction stove of inflammable gas etc.
The application advocates right of priority based on Japanese Patent Application 2010-095498 number that filed an application in Japan on April 16th, 2010, and its content is incorporated herein.
Background technology
In the past, for gasification is produced inflammable gas etc. effectively, studied the vapourizing furnace of the various formations such as fixed-bed type, fluidized bed type and air flow bed (fluid injected bed) type.For the vapourizing furnace of entrained flow type as one of them, particularly when being considered as the purposes of generating usefulness since high capacity easily, the reason such as load tracing ability height, become the main flow of vapourizing furnace in recent years.
In the vapourizing furnace of entrained flow type, the pyrolysis by coal produces coal tar take carbon as principal constituent (Char: not gasification of coal residue or pyrolysis residue), tar etc.In order to cut down this coal tar by gasification reaction, proposed to possess the vapourizing furnace (coal gasification reaction stove) (for example with reference to patent documentation 1) of two section two cell structure of the high-temperature gasification stove (bottom reaction vessel) that is located at hypomere and the pyrolytic gasification Reaktionsofen (top reaction vessel) that is located at epimere.
For this vapourizing furnace, by to the high-temperature gasification stove that is made as high temperature and high pressure with the ratio of regulation for coal supply, oxygen and water vapour, thereby pyrolysis of coal is produced coal tar take carbon as principal constituent, tar etc.In addition, by in the pyrolytic gasification Reaktionsofen of this vapourizing furnace, supplying with water vapour, thereby char gasification is cut down the growing amount of coal tar based on following chemical equation (1).
C (coal tar)+H
2O → CO+H
2(1)
The prior art document
Patent documentation
Patent documentation 1: TOHKEMY 2002-155289 communique
Summary of the invention
The technical problem that invention will solve
Yet, in the vapourizing furnace shown in the patent documentation 1, when generating coal tar, coal generates the high tar of viscosity, and this tar can be attached to the internal surface (carbonaceous material that is actually from tar is attached to internal surface) of pyrolytic gasification Reaktionsofen.The tar that generates reacts with supplying the water vapour to the pyrolytic gasification Reaktionsofen, is vaporized based on above-mentioned chemical equation (1).But owing to excessively supply with water vapour in the pyrolytic gasification Reaktionsofen, the amount that therefore can put into coal in the pyrolytic gasification Reaktionsofen etc. reduces, and produces the problem of the yield reducation of the inflammable gas in the vapourizing furnace.
The present invention finishes in view of such problem, and its purpose is to provide the output that can significantly not reduce inflammable gas, and can effectively be suppressed at method of operation and the coal gasification reaction stove of the coal gasification reaction stove that the adhesion amount of tar in the reaction vessel of top increases.
The means that are used for the technical solution problem
In order to achieve the above object, the method for operation of the coal gasification reaction stove of a scheme of the present invention is the method for operation that possesses the coal gasification reaction stove of the bottom reaction vessel that interconnects and top reaction vessel, and it has following operation.
Operation to internal feed carbon raw material, oxygen and the water vapour of above-mentioned bottom reaction vessel.
The operation of steam jet supply water vapour to the inside of above-mentioned top reaction vessel, when using the coal nozzle for coal supply.
Utilization makes the above-mentioned coal of the inside of above-mentioned top reaction vessel react to make the operation of the synthesis gas that contains at least hydrogen and CO (carbon monoxide converter) gas under the temperature more than 950 ℃ at the gas of the high temperature that the inside of above-mentioned bottom reaction vessel generates.
Ask the operation of counting the mass rate Qs that states the water vapour that contains in the synthesis gas in.
Ask the calculation confession to the operation of the mass rate Qc of the carbon of top reaction vessel based on the carbon content of above-mentioned coal.
With the ratio Qs/Qc of the mass rate Qs of above-mentioned water vapour and the mass rate Qc of above-mentioned carbon reach more than 1.0 and the mass rate of 1.5 following modes, the mass rate of regulating the above-mentioned coal that above-mentioned coal nozzle supplied with and the above-mentioned water vapour that above-mentioned steam jet is supplied with at least one party's operation.
According to above-mentioned method of operation, be more than 1.0 by making than Qs/Qc, can supply with is enough to and will passes through the water vapour of the pyrogenous origin tar gasification of coal in bottom reaction vessel and top reaction vessel.Therefore, can effectively be suppressed at the adhesion amount increase of tar in the reaction vessel of top.In addition, be below 1.5 by making than Qs/Qc, can prevent from the reaction vessel of top, excessively supplying with water vapour and prevent that the output of synthesis gas from significantly reducing.
The method of operation of the coal gasification reaction stove of a scheme of the present invention is used bottom reaction vessel and top reaction vessel, described bottom reaction vessel is formed with accommodation space in inside, described top reaction vessel is located at the top of above-mentioned bottom reaction vessel, and is formed with the through hole that is situated between and is communicated with the above-mentioned accommodation space of above-mentioned bottom reaction vessel and is extended along the vertical direction by reducing diameter part.Ratio with regulation is supplied with carbon raw material, oxygen and water vapour to above-mentioned bottom reaction vessel.Supply coal supply and water vapour to above-mentioned top reaction vessel.Then, be used to the high-temperature gas sensible heat from above-mentioned bottom reaction vessel, above-mentioned coal reacted under the temperature more than 950 ℃ in the reaction vessel of above-mentioned top, thereby make at least hydrogen and CO (carbon monoxide converter) gas.In the method for operation of such coal gasification reaction stove, the quality of the above-mentioned water vapour that contains from the fluid that the outlet of the above-mentioned through hole of above-mentioned top reaction vessel is flowed out with time per unit and every above-mentioned unit time reach mode 1.0 or more and 1.5 below for the mass ratio of the carbon to the above-mentioned coal of above-mentioned top reaction vessel, and adjusting supplies the extremely above-mentioned coal of above-mentioned top reaction vessel and the mass rate of at least one party in the above-mentioned water vapour.
In addition, as above-mentioned carbon raw material, such as using coal, coal tar etc. to contain the solid matter of carbon.
The pyrolysis by coal in bottom reaction vessel and top reaction vessel of coal gasification reaction stove becomes tar next life.Time per unit is made as Qc for the mass rate of the carbon to the coal of top reaction vessel, and the mass rate of the water vapour that time per unit is contained from the fluid that the outlet of the through hole of top reaction vessel is flowed out is made as Qs.Their ratio Qs/Qc is called " water vapour/carbon mass ratio ".Reach more than 1.0 and 1.5 following modes with this water vapour/carbon mass ratio, regulate supplying to the coal of top reaction vessel and the mass rate of at least one party in the water vapour.At this moment, owing in the reaction vessel of top, under the temperature more than 950 ℃, react, therefore cause easily the gasification reaction of tar.
The inventor finds, by water vapour/carbon mass ratio is adjusted to 1.0, be attached to the top reaction vessel through hole inner peripheral surface tar amount be attached in advance through hole and reach balanced by the amount of removing that the reaction with water vapour becomes the tar of carbon monoxide.
To the top reaction vessel, not only supply with directly for the water vapour to the top reaction vessel, also supply with by the water vapour that generates for the coal to top reaction vessel and heating, from the accommodation space of the bottom reaction vessel water vapour as the gas outflow.Such water vapour can react with carbon and resolve into CO (carbon monoxide converter) gas and hydrogen.Here, water vapour/carbon mass ratio is 1.0 state refers to exist a certain amount of remaining water vapour that is not consumed by the reaction with carbon in the reaction vessel of top state.
Like this, be more than 1.0 by making water vapour/carbon mass ratio, the adhesion amount that can effectively suppress the tar in the reaction vessel of top increases.In addition, by water vapour/carbon mass ratio is adjusted to below 1.5, thereby can prevent from the reaction vessel of top, excessively supplying with the yield reducation that water vapour prevents inflammable gas.
In addition, in the method for operation of above-mentioned coal gasification reaction stove, can ask as getting off the quality of calculating the above-mentioned water vapour that every above-mentioned unit time contains from the fluid that the outlet of the above-mentioned through hole of above-mentioned top reaction vessel is flowed out.Measure the mass rate of the above-mentioned fluid of every above-mentioned unit time outflow.Measure the water vapor concentration that contains in the above-mentioned fluid.The quality of the above-mentioned water vapour that contains in the fluid of product as every above-mentioned unit time outflow of the value that the value that then, the above-mentioned mass rate of mensuration is obtained and the above-mentioned water vapor concentration of mensuration obtain.
According to the method, can easily ask the quality of calculating the water vapour that time per unit contains from the fluid that the outlet of through hole is flowed out.
In addition, in the method for operation of above-mentioned coal gasification reaction stove, can be by the internal feed water vapour of following mode to above-mentioned top reaction vessel.At first, measure pressure difference between the end of top of the accommodation space of the part of below of the coal nozzle of supplying with above-mentioned coal in the through hole of above-mentioned top reaction vessel or above-mentioned bottom reaction vessel and above-mentioned through hole.Then, when above-mentioned pressure difference surpasses the value of regulation, to the water vapour of the amount of the internal feed regulation of above-mentioned top reaction vessel.
According to the method, can prevent more positively that the through hole of top reaction vessel from being stopped up by tar.
In addition, the coal gasification reaction stove of a scheme of the present invention is the coal gasification reaction stove that uses in above-mentioned method of operation.This coal gasification reaction stove and accessory standby inside be formed with the bottom reaction vessel of accommodation space and be located at above-mentioned bottom reaction vessel above the top reaction vessel.The gasification burner tip (pulverizing jet) that the ratio that above-mentioned bottom reaction vessel has to stipulate is supplied with carbon raw material, oxygen and water vapour and above-mentioned carbon raw material is burnt to above-mentioned bottom reaction vessel.Above-mentioned top reaction vessel has: the through hole that is situated between and is communicated with the above-mentioned accommodation space of above-mentioned bottom reaction vessel and is extended along the vertical direction by reducing diameter part; Coal nozzle to the internal feed coal; Steam jet to internal feed water vapour; And be located at above-mentioned through hole the top the end and measure the amount of moisture determinator of the quality of the water vapour that time per unit flows out from the end of above-mentioned through hole.
The pyrolysis by coal in bottom reaction vessel and top reaction vessel of this coal gasification reaction stove becomes tar next life.In the reaction vessel of top, tar and water vapour react under the temperature more than 950 ℃.In addition, the amount of moisture determinator is measured time per unit from the quality of the water vapour of the end outflow of the top of through hole.Then, reach more than 1.0 with above-mentioned water vapour/carbon mass ratio and 1.5 following modes are regulated at least one party in coal nozzle and the steam jet.Thus, can keep the output of inflammable gas, and effectively suppress the adhesion amount increase of the tar in the reaction vessel of top.
In addition, above-mentioned coal gasification reaction stove can possess the first pipe arrangement, the second pipe arrangement and pressure measuring unit.The part of the below of above-mentioned coal nozzle or the accommodation space of above-mentioned bottom reaction vessel are connected in the through hole of above-mentioned the first pipe arrangement and above-mentioned top reaction vessel.Above-mentioned the second pipe arrangement is connected with the end of the top of the above-mentioned through hole of above-mentioned top reaction vessel.Above-mentioned pressure measuring unit is measured the pressure difference of above-mentioned the first pipe arrangement and above-mentioned the second pipe arrangement.
The inventor finds, because the tar that the pyrolysis of coal generates can be concentrated the prescribed position of the top of coal nozzle in the through hole that is attached to the top reaction vessel.
Find that based on this end of the top of the accommodation space of the part of the below of spray nozzle part or bottom reaction vessel and through hole is connected in through hole of the top reaction vessel that each pipe arrangement and tar are difficult to adhere to.Thus, can prevent that tar is attached to pipe arrangement and measures exactly pressure difference.
The invention effect
According to method of operation and the coal gasification reaction stove of the coal gasification reaction stove of such scheme, can keep the output of inflammable gas, and the adhesion amount that effectively is suppressed at tar in the reaction vessel of top increases.
Description of drawings
Fig. 1 is the block diagram of gasification system that comprises the coal gasification reaction stove of the present invention's the 1st embodiment.
Fig. 2 is the synoptic diagram of section of the coal gasification reaction stove of the present invention's the 1st embodiment.
Fig. 3 is that each value in the coal gasification reaction stove of expression the present invention the 1st embodiment is with respect to the figure of the variation of water vapour/carbon mass ratio.
Fig. 4 is the synoptic diagram of section of the coal gasification reaction stove of the present invention's the 2nd embodiment.
Pressure difference was with respect to the figure of the variation in elapsed time when Fig. 5 was the coal gasification reaction stove of expression running the present invention the 2nd embodiment.
Embodiment
(the 1st embodiment)
Below, referring to figs. 1 through Fig. 3 the coal gasification reaction stove of the present invention's the 1st embodiment is described.The coal gasification reaction stove of present embodiment is the part of gasification system, is by making coal make at least the device of hydrogen and CO (carbon monoxide converter) gas in internal-combustion.
As shown in Figure 1, gasification system 1 is to synthesize the synthesis gas take hydrogen and CO (carbon monoxide converter) gas as principal constituent as raw material and finally made the suite of equipment of the products such as methane, methyl alcohol and ammonia by this synthesis gas with coal.
Usually, the external diameter of coal is inhomogeneous, sometimes contains than the more moisture of desired value according to the difference of its kind.For this reason, at first in coal pulverizer and drying plant 2, it for example is granular about following of the above and 100 μ m of 10 μ m that coal is ground into particle diameter (external diameter).Coal after the pulverizing further is dried to reach after the moisture content of regulation for to coal supply arrangement 3.In addition, till put into coal gasification reaction stove 4, coal was mobile in airtight space, so that the amount of moisture in the dried coal does not change after coal was discharged from coal pulverizer and drying plant 2.
Then, can be for the state to coal gasification reaction stove 4 in order to become, after coal mixes with carrier gas and boosts to the pressure of regulation, be sent to coal gasification reaction stove 4 by transmission in coal supply arrangement 3.In addition, not only supply coal supply from the gasification burner tip described later 17 of coal gasification reaction stove 4, also supply with the solid matter of the carbon containing such as coal tar by the not shown supply mean that goes out.Below, the solid matter of the carbon containings such as coal, coal tar is called " carbon raw material ".
As depicted in figs. 1 and 2, coal gasification reaction stove 4 possesses the partial oxidation section (bottom reaction vessel) 11 that is formed with accommodation space 11a in inside and the pyrolysis section (top reaction vessel) 13 that is located at the top D1 of partial oxidation section 11.Be formed with via reducing diameter part 13a in pyrolysis section 13 and be communicated with the accommodation space 11a of partial oxidation section 11 and the through hole (tube) 12 that extends of D along the vertical direction.Coal gasification reaction stove 4 is for example formed by stable on heating brick.
By reducing diameter part 13a is set, partial oxidation section 11 and pyrolysis section 13 independently can operated under the reaction conditions separately.
D2 is provided with cooling of furnace slag tank 14 below in the vertical direction of partial oxidation section 11.Partial oxidation section 11 and cooling of furnace slag tank 14 are communicated with at above-below direction (vertical direction) D.Connection portion at partial oxidation section 11 and cooling of furnace slag tank 14 is formed with the 2nd reducing diameter part 14a.
As shown in Figure 2, partial oxidation section 11 forms the roughly cylindric of along the vertical direction D extension.On the inner peripheral surface of partial oxidation section 11, be provided with a plurality of gasification burner tips cylindraceous 17 that extend along the axis C1 of regulation that form.Gasification burner tip 17 and coal supply arrangement 3 shown in Figure 1, air separation equipment 10 and be connected with the heat recovery equipment 5 that method described later generates water vapour.This gasification burner tip 17 can be supplied with carbon raw material, oxygen and water vapour (hereinafter referred to as " carbon raw material etc. ") with the ratio of regulation to partial oxidation section 11.Gasification burner tip 17 disposes in the following manner: its axis C1 with respect to the horizontal plane and front towards oblique below, and with respect to central axis C 2 position for reversing of partial oxidation section 11.
In addition, be provided with the not shown cooling way that goes out at the periphery of partial oxidation section 11, can be because of 11 coolings of the heated partial oxidation of burning of coal section.
In pyrolysis section 13, at the pars intermedia of above-below direction D a plurality of coal nozzles 18 for coal supplies to pyrolysis section 13 are set, D2 is provided with 1 steam jet 19 from water vapour to pyrolysis section 13 that supply with below coal nozzle 18.Coal nozzle 18 is connected with coal supply arrangement 3, and steam jet 19 is connected with heat recovery equipment 5.
In addition, the quantity of coal nozzle 18 and steam jet 19 severally all can without limits.
End (outlet) 12a of the top D1 of the through hole 12 of pyrolysis section 13 is connected with heat recovery equipment 5.
Be provided with the amount of moisture determinator 20 of the quality of measuring the water vapour that time per unit (for example per 1 hour) flows out from the end 12a of through hole 12 at the end 12a of the through hole 12 of pyrolysis section 13.
Amount of moisture determinator 20 can be by will measuring the synthesis gas that time per unit flows out from the end 12a of through hole 12 mass rate under meter and the ratio (water vapor concentration) of measuring the water vapour that contains this synthesis gas the combination such as Atomic Absorption SpectrophotometerICP and utilize known technology to consist of.The quality (mass rate Qs) of the water vapour that above-mentioned time per unit flows out such as the value that can be obtained by the mass rate of measuring synthesis gas with under meter is asked calculation with the product with the value of the water vapor concentration of the mensuration such as Atomic Absorption SpectrophotometerICP.
In cooling of furnace slag tank 14, take in the water W of specified amount.The cooling of furnace slag such as described later, that cooling of furnace slag tank 14 will flow down from partial oxidation section 11.
Then, the method for operation of coal gasification reaction stove 4 described.
The carbon raw material etc. that at first, will contain Paniculate coal by gasification burner tip 17 with the flow velocity of regulation for to partial oxidation section 11.Each gasification burner tip 17 is configured on the position of reversing with respect to axis C2 as mentioned above like that.Therefore, the equilateral D2 downwards of carbon raw material that supplies with from each gasification burner tip 17 moves the limit and rotates in the shape of a spiral around the central axis C 2 of partial oxidation section 11.At this moment, for example be that temperature is more than 1300 ℃ and the high temperature below 1700 ℃, pressure are the high pressure that 2MPa is above and 3MPa is following in the partial oxidation section 11.Carbon raw material becomes high temperature and pyrolysis occurs under this environment, coal tar with contain the volatile gases of tar with water vapour etc. and separate.In addition, carbon raw material burns, and generates CO (carbon monoxide converter) gas, carbon dioxide and hydrogen and the slag (ash content) of high temperature based on the chemical reaction shown in following chemical equation (2)～(4).
2C＋O
2→2CO (2)
C＋O
2→CO
2 (3)
C＋H
2O→CO＋H
2 (4)
The heat that generates when the gas of partial oxidation section 11 interior generations, slag etc. burn because of carbon raw material becomes high temperature and expands, be subject to D1 upward buoyancy and while rotating in the 11 interior risings of partial oxidation section.
Slag in the 11 interior generations of partial oxidation section is the state of melting.The part of this slag is cooled off postadhesion at the inner peripheral surface of partial oxidation section 11 on this inner peripheral surface by above-mentioned cooling way, and the water W that another part falls in the cooling of furnace slag tank 14 that is located at partial oxidation section 11 belows are cooled, reclaim.
Move and in the 13 interior risings of pyrolysis section from partial oxidation section 11 at the gases such as water vapour of the high temperature of partial oxidation section 11 interior generations, tar, coal tar etc.In the present embodiment, the temperature in the pyrolysis section 13 is adjusted to the temperature more than 950 ℃.When the temperature in the pyrolysis section 13 was lower than 950 ℃, the growing amount of tar can sharply increase, and became and be difficult to occur the decomposition reaction of tar.
At this moment, respectively from coal nozzle 18 for coal supply, from steam jet 19 supply water vapour.Operator regulate at least one party's of above-mentioned coal and water vapour feed rate in the following manner.That is, time per unit (for example per 1 hour) is made as Qc from whole coal nozzle 18 for the quality of the carbon to the coal of pyrolysis section 13.The quality of the water vapour that in addition, time per unit (for example per 1 hour) is contained from the fluid of the end 12a outflow of through hole 12 is made as Qs.Be that water vapour/carbon mass ratio is adjusted to more than 1.0 and below 1.5 with their ratio Qs/Qc.
For be not only the water vapour of supplying with from steam jet 19 to the water vapour of pyrolysis section 13, also comprise the water vapour that the moisture gasification that contains the water vapour that flows into from the accommodation space 11a of partial oxidation section 11, the coal forms.Therefore, regulate for the amount of the water vapour that flows out based on the end 12a from through hole 12 to the water vapour of pyrolysis section 13.For reacting to the water vapour of pyrolysis section 13 and carbon and generating CO (carbon monoxide converter) gas and hydrogen.Water vapour/carbon mass ratio is that 1.0 state is the state that has a certain amount of remaining water vapour that has not reacted with carbon in pyrolysis section 13.
Above-mentioned water vapour/carbonaceous amount ratio is as adopting following method to regulate.At first, by amount of moisture determinator 20, the quality of the water vapour that the mensuration time per unit contains from the end 12a effluent air of the through hole 12 of pyrolysis section 13.For example, when the mass rate Qs of the water vapour that records is that 100 (kg/h), water vapour/carbon mass ratio are 1.0 when above, reach mode below 100 (kg/h) to regulating for the mass rate to the coal of pyrolysis section 13 from whole coal nozzle 18 for the mass rate Qc to the carbon of pyrolysis section 13.That is to say, when being provided with 2 coal nozzles 18, for example to reach mode 50 (kg/h) below to regulating from each coal nozzle 18 confessions to mass rate of the coal of pyrolysis section 13 from each coal nozzle 18 for the mass rate Qc to the carbon of pyrolysis section 13.
At this moment, measure in advance for the carbon content to the coal of pyrolysis section 13, and grasp in advance the relation of the mass rate Qc of the mass rate of coal and carbon.Thus, can determine to make water vapour/carbon mass ratio is the mass rate of 1.0～1.5 needed coals.
In addition since from coal nozzle 18 for coal supplies, therefore sometimes can change with the mass rate Qs of the water vapour of amount of moisture determinator 20 mensuration.In this case, the mass rate of the coal supplied with is regulated, again with the mass rate Qs of the water vapour that contains in the amount of moisture determinator 20 mensuration synthesis gass.And, for the water vapour of keeping regulation/carbon mass ratio, repeatedly carry out the mensuration of the mass rate Qs of the adjusting of mass rate of coal and water vapour.
In addition, in this embodiment, although only the mass rate of coal is regulated, according to condition, also can be to regulating from steam jet 19 confessions to the mass rate of the water vapour of the accommodation space 11a of partial oxidation section 11.In addition, can also be in the mass rate of regulating coal, to regulating from gasification burner tip 17 confessions to the mass rate of the water vapour of the accommodation space 11a of partial oxidation section 11.In addition, also can make the mass rate of coal constant, and to regulating from steam jet 19 or gasification burner tip 17 confessions to the mass rate of the water vapour of the accommodation space 11a of partial oxidation section 11.
In addition, when the mass rate that makes the coal of supplying with from coal nozzle 18 increases, make in advance the mass rate of the water vapour of supplying with from steam jet 19 increase to suitable value.And, after the stable reaction in pyrolysis section 13, utilize amount of moisture determinator 20 to measure the mass rate Qs of the water vapour that contains in the synthesis gas.
Then, as long as the mass rate of the coal supplied with from coal nozzle 18 is regulated to satisfy above-mentioned water vapour/carbon mass ratio.
In addition, amount of moisture determinator 20 can use various determinators, also can replace with dew point hygrometer.
The part of the tar that in the past, generated in the partial oxidation section 11 and the carbon generation pyrolysis supplied with from coal nozzle 18 and the part of the tar that generates becomes the carbonaceous material of tack sometimes in the through hole 12 of pyrolysis section 13 and be attached to the inner peripheral surface of through hole 12.
But in the present embodiment, the ratio Qs/Qc with the quality of carbon regulates as mentioned above like that for the quality of the water vapour to pyrolysis section 13.Therefore, the tar of inner peripheral surface that in the past was attached to the through hole 12 of pyrolysis section 13 can become gas based on following chemical equation (5), and flows out from pyrolysis section 13.
C (tar)+H
2O → CO+H
2(5)
Fig. 3 is the chart of relation of the variation of gathering way of the expression water vapour/variation of carbon mass ratio and the adhesion amount of tar and energy efficiency.Transverse axis represents water vapour/carbon mass ratio, and the longitudinal axis in left side represents the gathering way of adhesion amount of the tar in the through hole 12 of pyrolysis section 13, and the longitudinal axis on right side represents energy efficiency.In addition, energy efficiency described here is the ratio of following 2 thermal values.That is: the carbon raw material of supplying with from the coal nozzle 18 of the gasification burner tip 17 of partial oxidation section 11 and pyrolysis section 13 and the thermal value of coal, with coal gasification reaction stove 4 ratio of thermal value of the gases such as the hydrogen that obtains and carbon monoxide, oil.
When water vapour/carbon mass ratio greater than 1.0 the time, gathering way of the adhesion amount of the tar shown in the solid line L1 is negative value in Fig. 3, the amount of tar that is attached to the inner peripheral surface of pyrolysis section 13 reduces.On the other hand, when water vapour/carbon mass ratio less than 1.0 the time, the adhesion amount of tar gather way on the occasion of, the adhesion amount of the tar of the inner peripheral surface of pyrolysis section 13 increases.
In addition, water vapour/carbon mass ratio is larger, is attached to easier the removing of tar of pyrolysis section 13 based on above-mentioned chemical equation (5).But when the amount of water vapour was too much, the temperature in the pyrolysis section 13 can reduce, and the carbon raw material that can put in the pyrolysis section 13 reduces, and the energy efficiency in Fig. 3 shown in the dotted line L2 reduces.In order to make energy efficiency reduction within reason, preferably be made as the value of water vapour/carbon mass ratio more than 1.0 and below 1.5.In addition, when the higher energy efficiency of needs, the value of water vapour/carbon mass ratio can be made as more than 1.0 and below 1.1.
In addition, react for the part of the carbon to the coal of pyrolysis section 13 and the carbon dioxide in the pyrolysis section 13, become CO (carbon monoxide converter) gas based on following chemical equation (6).
C＋CO
2→2CO (6)
Then, as shown in Figure 1, from the top of pyrolysis section 13, the synthesis gas take hydrogen and CO (carbon monoxide converter) gas as the high temperature of principal constituent is transmitted with coal tar and supplies to heat recovery equipment 5.
In heat recovery equipment 5, come the heating water steam by making the synthesis gas that transmits from pyrolysis section 13 and water vapour carry out heat exchange.This water vapour is conducted to the purposes such as drying that above-mentioned coal pulverizer and drying plant 2, coal gasification reaction stove 4 etc. are used for coal.
Cooled synthesis gas supplies to coal tar recovery system 6 from heat recovery equipment 5 in heat recovery equipment 5.In coal tar recovery system 6, the coal tar that contains in the synthesis gas is recovered.
Supply to transformationreation equipment 7 by the synthesis gas behind the coal tar recovery system 6.In transformationreation equipment 7, for hydrogen in the synthesis gas is brought up to certain value and supplied with water vapour with respect to the ratio of CO (carbon monoxide converter) gas.Then, based on the transformationreation shown in the following chemical equation (7), generate carbon dioxide and hydrogen by the CO (carbon monoxide converter) gas in the synthesis gas and water vapour.
CO＋H
2O→CO
2＋H
2 (7)
The synthesis gas of having regulated composition in transformationreation equipment 7 is for to gas refinishing equipment 8, the carbon dioxide that contains in the synthesis gas, contains sulphur and is recovered as the gas of composition etc.
Synthesis gas after refining in gas refinishing equipment 8 is made the products such as methane, methyl alcohol for to chemosynthesis equipment 9.
As discussed above, in the method for operation of the coal gasification reaction stove 4 of present embodiment and coal gasification reaction stove 4, to for regulating to the coal of pyrolysis section 13 and at least one party's in the water vapour mass rate so that water vapour/carbon mass ratio reaches more than 1.0 and below 1.5.
The inventor finds, by water vapour/carbon mass ratio is adjusted to 1.0, be attached to the tar in the through hole 12 of pyrolysis section 13 amount, be attached in advance through hole 12 and become the amount of the removing equilibrium of the tar of carbon monoxide by the reaction with the above-mentioned chemical equation (5) of water vapour.
Based on this discovery, in the above-mentioned embodiment water vapour/carbon mass ratio is set as more than 1.0.Thus, even generated tar in partial oxidation section 11 and pyrolysis section 13 because of the pyrolysis of coal, the through hole 12 coal-tar middle oil adhesion amounts that also can effectively be suppressed at pyrolysis section 13 increase.
In addition, by water vapour/carbon mass ratio is adjusted to below 1.5, can prevent that water vapour is by excessively for to pyrolysis section 13 and make the yield reducation of the inflammable gas such as hydrogen.
In addition, in the above-described embodiment, when asking the quality of calculating the water vapour that time per unit contains from the fluid that the end 12a of the through hole 12 of pyrolysis section 13 flows out, measure the mass rate of the fluid that time per unit flows out, measure the water vapor concentration that contains in the fluid.And, the quality of the water vapour that contains in the fluid that the value that the quality measurement flow is obtained and the product of measuring the value that water vapor concentration obtains flow out as time per unit.
Therefore, can easily ask the quality of calculating the water vapour that time per unit contains from the fluid that the end 12a of through hole 12 flows out.
(the 2nd embodiment)
Then, the 2nd embodiment of the present invention is described.Below, also the description thereof will be omitted to give identical symbol to the position identical with the 1st embodiment, only the aspect different from the 1st embodiment described.
As shown in Figure 4, the coal gasification reaction stove 31 of present embodiment also further possesses the pressure measuring unit 32 of the pressure difference of measuring pyrolysis section 13 except each formation of the coal gasification reaction stove 4 of the 1st embodiment.
When the coal gasification reaction stove 31 of formation like this turns round, in the adjusting of the coal of supplying with from coal nozzle 18 and steam jet 19 that operator illustrated and the mass rate of at least one party the water vapour, carry out following operation in carrying out above-mentioned the 1st embodiment.
That is, regularly or continuously measure the pressure difference of the first pipe arrangement 33 and the second pipe arrangement 34 with pressure measuring unit 32.Then, when the pressure difference that records surpasses the benchmark value of regulation, the water vapour of the mass rate of the internal feed regulation from steam jet 19 to pyrolysis section 13.
The example of result when Fig. 5 shows the pressure difference of practical measurement pyrolysis section 13.The transverse axis of Fig. 5 represents the elapsed time (min), and the pressure difference (with the variable quantity of common pressure difference) that the longitudinal axis represents the first pipe arrangement 33 and the second pipe arrangement 34 (kPa).
Along with the process of time, tar is attached to the inner peripheral surface of pyrolysis section 13 gradually, and pressure difference begins to rise when moment T0, and pressure difference reaches benchmark value 10 (kPa) when moment T1.This moment is 13 water vapour of supplying with specified amounts from steam jet 19 to pyrolysis section.Here the water vapour of so-called specified amount for example be per 1 hour from coal nozzle 18 to pyrolysis section about 5～10% mass rate of the amount of 13 coals that drop into.
Consequently, the tar that is attached to pyrolysis section 13 reduces, and pressure difference is reduced to common pressure difference.
In addition, even when the water vapour of 5～10% mass rate of the amount of supplying with the coal that dropped in per 1 hour, when pressure difference is not reduced to common value yet, can further supply with the water vapour of about 5% quality of amount of the coal of per 1 hour input.At this moment, water vapour/carbon mass ratio does not need to be defined as 1.0～1.5 scope.But, after pressure difference is reduced to common pressure difference, preferably in water vapour/carbon mass ratio is 1.0～1.5 scope, turn round.
As discussed above, according to the coal gasification reaction stove 31 of present embodiment, because the mass rate of the water vapour of supplying with can too not increase, therefore can keep the output of inflammable gas.In addition, by supply with the water vapour of enough mass rates to the gasification reaction of tar, the adhesion amount that can effectively suppress the tar in the pyrolysis section 13 increases.
In addition, the inventor finds, tar is concentrated the position (for example the top D1 of coal nozzle 18 is apart from the position of coal nozzle 18 hundreds of mm) of regulation of the top D1 of the coal nozzle 18 in the through hole 12 that is attached to pyrolysis section 13.Based on this discovery, in the above-described embodiment, pipe arrangement 33 and 34 is connected to the below D2 of the coal nozzle 18 that tar is difficult for adhering to and the end 12a of through hole 12.Thus, can prevent that tar is attached to pipe arrangement 33 and 34 and measure exactly pressure difference, can prevent more positively that the through hole 12 of pyrolysis section 13 from being stopped up by tar.
In addition, because the part of the below D2 of the coal nozzle 18 in the through hole 12 of pyrolysis section 13 also is difficult for adhering to tar, therefore also can connect the first pipe arrangement 33 in this part.
More than, 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 change etc. of the formation of the scope that does not break away from purport of the present invention.
For example, in the 1st embodiment and the 2nd embodiment, also can in the coal gasification reaction stove, not possess amount of moisture determinator 20, and by the following coal gasification reaction stove that turns round like that illustratedly.That is, ask the carbon amount of calculating in steam vapour amount and coal and the carbon raw material by calculating in advance, supply coal supply, supply with water vapour by steam jet 19 by coal nozzle 18 to pyrolysis section 13 based on this calculated value.About the amount of the water vapour that generates in the partial oxidation section 11, by obtaining the revenue and expenditure of oxygen, hydrogen, carbon based on amount, the composition of carbon raw material, the amount of oxygen and the amount of water vapour of the carbon raw material that drops into, thereby can calculate with precision to a certain degree.About the water vapour in pyrolysis section 13 exits/carbon mass ratio, can based on the input amount of the input amount of the coal in the pyrolysis section 13, water vapour, because of with coal in the disappearance amount of the water vapour that causes of the water vapour reaction of carbon calculate.In addition, the carbon amount in the coal can adopt the method for stipulating among the JIS M8819 to measure.
When so not possessing amount of moisture determinator 20, can produce flow change and the flow error of coal, carbon raw material and water vapour.Therefore, above-mentioned water vapour/carbon mass ratio need to be made as water vapour/carbon mass ratio and be far longer than 1.0 value (for example 1.2 or more and below 1.5) less than 1.0 danger in the running.
Embodiment
(embodiment 1)
Use the device of Fig. 1, test with the coal of the drying that contains 3% moisture, 71.8% carbon.This coal not only is used for pyrolysis section 13, also as the carbon raw material that supplies to partial oxidation section 11.
Mass rate from 17 confessions of whole gasification burner tips to the coal of partial oxidation section 11 is that the flow of 650 (kg/h), oxygen is 385 (Nm
3/ h), the mass rate of water vapour is 60 (kg/h).In addition, from whole coal nozzle 18 for the mass rate to the coal of pyrolysis section 13 be 150 (kg/h), the mass rate of the water vapour that drops into from steam jet 19 is 60 (kg/h).
At this moment, the concentration of the water vapour that contains the synthesis gas that the end 12a from through hole 12 that records with amount of moisture determinator 20 flows out is 8.1% (volume %), and the flow that generates gas is counted 1760 (Nm with dry flow
3/ h).Then, the mass rate of the water vapour that the mass rate Qc that tries to achieve the carbon that time per unit contains from the coal that whole coal nozzle 18 is supplied with is 104 (kg/h), flow out from the end 12a of through hole 12 is 125 (kg/h), and water vapour/carbon mass ratio is 1.2.
Under above-mentioned operating condition (water vapour/carbon mass ratio is 1.2), temporarily shutting down after the running in 100 hours and after the running in 200 hours, pyrolysis section 13 inside are investigated.At this moment, there be not to find adhering to from the carbonaceous material of tar.
(embodiment 2)
Use the device of Fig. 4, test with the coal of the drying that contains 3% moisture, 71.8% carbon.This coal not only is used for pyrolysis section 13, also as the carbon raw material that supplies to partial oxidation section 11.
Mass rate from 17 confessions of whole gasification burner tips to the coal of partial oxidation section 11 is that the flow of 650 (kg/h), oxygen is 385 (Nm
3/ h), the mass rate of water vapour is 60 (kg/h).In addition, from whole coal nozzle 18 for the mass rate to the coal of pyrolysis section 13 be 150 (kg/h), the mass rate of the water vapour that drops into from steam jet 19 is 40 (kg/h).On calculating, be that water vapour/carbon mass ratio reaches 1.0 condition.
But, because the moisture change in the coal, make moisture in the coal be lower than 3% coal and temporarily be put into, therefore the pressure difference of the first pipe arrangement 33 and the second pipe arrangement 34 rises gradually.When pressure difference increased by 50% with respect to the pressure difference of start of run, the mass rate of putting into the water vapour the pyrolysis section 13 from steam jet 19 increased to 60 (kg/h).Therefore then, pressure difference reduces gradually, is lower than for 10% stage in pressure difference with respect to the pressure difference of start of run, and the mass rate of putting into the water vapour the pyrolysis section 13 from steam jet 19 is reduced to 50 (kg/h).Then, after running in 100 hours, with the rear temporary transient shut-down operation of running in 200 hours, pyrolysis section 13 inside are investigated.At this moment, do not find adhering to from the carbonaceous material of tar.
(comparative example 1)
Mass rate, the flow of oxygen and the mass rate of water vapour of the coal of supplying with from whole gasification burner tip 17 are equated with embodiment 1.And the mass rate that makes the coal of supplying with from coal nozzle 18 is 160 (kg/h), the mass rate of the water vapour supplied with from steam jet 19 is 40 (kg/h).
At this moment, the concentration of the water vapour that records with amount of moisture determinator 20 is 6.7% (volumetric concentration), and the flow that generates gas is counted 1775 (Nm with dry flow
3/ h).Under this condition, as seen be attached to the increase of the tar in the pyrolysis section 13.
At this moment, the mass rate Qs of the water vapour that the mass rate Qc that tries to achieve the carbon that time per unit contains from the coal that coal nozzle 18 is supplied with is 111 (kg/h), flow out from the end 12a of through hole 12 is 102 (kg/h), and water vapour/carbon mass ratio is 0.92.
Under above-mentioned operating condition (water vapour/carbon mass ratio is 0.92), after running in 100 hours, with the rear temporary transient shut-down operation of running in 200 hours, pyrolysis section 13 inside are investigated.At this moment, confirm and produce adhering to of carbonaceous and increase.
(comparative example 2)
Mass rate, the flow of oxygen and the mass rate of water vapour of the coal of supplying with from whole gasification burner tip 17 are equated with embodiment 1.And the mass rate that makes the coal of supplying with from coal nozzle 18 is 125 (kg/h), the mass rate of the water vapour supplied with from steam jet 19 is 80 (kg/h).
At this moment, the concentration of the water vapour that records with amount of moisture determinator 20 is 9.0% (volumetric concentration), and the flow that generates gas is counted 1734 (Nm with dry flow
3/ h).Under this condition, in pyrolysis section 13, do not observe dirt settling.
At this moment, the mass rate Qs of the water vapour that the mass rate Qc that tries to achieve the carbon that time per unit contains from the coal that coal nozzle 18 is supplied with is 87 (kg/h), flow out from the end 12a of through hole 12 is 138 (kg/h), and water vapour/carbon mass ratio is 1.58.
In addition, in above-described embodiment and comparative example 1, comparative example 2, to putting into the coal in the pyrolysis section 13 and vapor volume has carried out adjusting so that the temperature of pyrolysis section 13 is constant (1100 ℃).
Gas generating amount in above-described embodiment is counted 1760 (Nm with dry flow
3/ h), thermal value is 8545 (kJ/Nm
3), the gas generating amount in the comparative example 1 is 1775 (Nm
3/ h), thermal value is 8593 (kJ/Nm
3), the gas generating amount in the comparative example 2 is 1734 (Nm
3/ h), thermal value is 8495 (kJ/Nm
3).In the embodiment of method of operation of the present invention, to compare with the comparative example 1 that has generated dirt settling in pyrolysis section, the gas volume of generation does not almost reduce, and thermal value also maintains and comparative example 1 level about equally.And, can under carbonaceous material is not attached to the situation of device, turn round.In addition, in the many comparative examples 2 of the amount that drops into water vapour, the coal amount of putting in the pyrolysis section reduces.Therefore, the gas volume of generation reduces.
More than, preferred implementation of the present invention is illustrated, but the invention is not restricted to above-mentioned embodiment or embodiment.In the scope that does not break away from purport of the present invention, what can consist of adds, omits, replaces and other change.The invention is not restricted to above-mentioned explanation, only limit to the scope of the claim of apposition.
The possibility of utilizing on the industry
According to method of operation and the coal gasification reaction stove of above-mentioned coal gasification reaction stove, the adhesion amount increase of tar in the reaction vessel of top can suppressed effectively in the situation that the output that does not make inflammable gas significantly reduces.
Nomenclature
4,31 coal gasification reaction stoves
11 partial oxidation sections (bottom reaction vessel)
12 through holes
The 12a end
13 pyrolysis sections (top reaction vessel)
The 13a reducing diameter part
17 gasification burner tips
18 coal nozzles
19 steam jet
20 amount of moisture determinators
32 pressure measuring units
33 first pipe arrangements
34 second pipe arrangements
Claims (6)
1. the method for operation of a coal gasification reaction stove is characterized in that,
Described coal gasification reaction stove and accessory is got section's reaction vessel and top reaction vessel ready, described bottom reaction vessel is formed with accommodation space in inside, described top reaction vessel is located at the top of described bottom reaction vessel, and be formed with to be situated between and be communicated with the described accommodation space of described bottom reaction vessel and the through hole of extension along the vertical direction by reducing diameter part
Ratio with regulation is supplied with carbon raw material, oxygen and water vapour to described bottom reaction vessel,
Supply coal supply and water vapour to described top reaction vessel,
Be used to the high-temperature gas sensible heat from described bottom reaction vessel, described coal reacted under the temperature more than 950 ℃ in the reaction vessel of described top, thereby make at least hydrogen and CO (carbon monoxide converter) gas,
Wherein, the quality of the described water vapour that contains from the fluid that the outlet of the described through hole of described top reaction vessel is flowed out with time per unit and every described unit time reach mode 1.0 or more and 1.5 below for the mass ratio of the carbon to the described coal of described top reaction vessel, and adjusting supplies the extremely described coal of described top reaction vessel and the mass rate of at least one party in the described water vapour.
2. the method for operation of coal gasification reaction stove according to claim 1 is characterized in that,
When asking the quality of calculating the described water vapour that every described unit time contains from the fluid that the outlet of the described through hole of described top reaction vessel is flowed out,
Measure the mass rate of the described fluid of every described unit time outflow,
Measure the water vapor concentration that contains in the described fluid,
The quality of the described water vapour that contains in the fluid that value that described mass rate obtains and the product of measuring the value that described water vapor concentration obtains flow out as every described unit time will be measured.
3. the method for operation of coal gasification reaction stove according to claim 1 and 2 is characterized in that,
Measure the pressure difference between the end of top of the accommodation space of the below part of the coal nozzle of supplying with described coal in the through hole of described top reaction vessel or described bottom reaction vessel and described through hole,
When described pressure difference surpasses the value of regulation, to the water vapour of the amount of the internal feed regulation of described top reaction vessel.
4. a coal gasification reaction stove is characterized in that,
It is the coal gasification reaction stove that uses in the method for operation of each described coal gasification reaction stove in claim 1～3,
It possesses bottom reaction vessel and top reaction vessel, described bottom reaction vessel is formed with accommodation space in inside, described top reaction vessel is located at the top of described bottom reaction vessel, and be formed with to be situated between and be communicated with the described accommodation space of described bottom reaction vessel and the through hole of extension along the vertical direction by reducing diameter part
The gasification burner tip that the ratio that described bottom reaction vessel has to stipulate is supplied with carbon raw material, oxygen and water vapour and described carbon raw material is burnt to described bottom reaction vessel,
Described top reaction vessel has:
To the coal nozzle of described top reaction vessel for coal supply;
Supply with the steam jet of water vapour to described top reaction vessel; With
Be located at described top reaction vessel described through hole the top the end and measure the amount of moisture determinator of the quality of the water vapour that time per unit flows out from the end of described through hole.
5. coal gasification reaction stove according to claim 4 is characterized in that having:
The first pipe arrangement, its with the through hole of described top reaction vessel in the part of below of described coal nozzle or the accommodation space of described bottom reaction vessel be connected; With
The second pipe arrangement, its end with the top of the described through hole of described top reaction vessel is connected,
The pressure measuring unit that further possesses the pressure difference of measuring described the first pipe arrangement and described the second pipe arrangement.
6. the method for operation of a coal gasification reaction stove, it is the method for operation that possesses the coal gasification reaction stove of the bottom reaction vessel that interconnects and top reaction vessel, has following operation:
Operation to internal feed carbon raw material, oxygen and the water vapour of described bottom reaction vessel;
The operation of steam jet supply water vapour to the inside of described top reaction vessel, when using the coal nozzle for coal supply;
Utilization makes the described coal of the inside of described top reaction vessel react to make the operation of the synthesis gas that contains at least hydrogen and CO (carbon monoxide converter) gas under the temperature more than 950 ℃ at the gas of the high temperature that the inside of described bottom reaction vessel generates;
Ask the operation of the mass rate Qs that calculates the water vapour that contains in the described synthesis gas;
Ask the calculation confession to the operation of the mass rate Qc of the carbon of the inside of top reaction vessel based on the carbon content of described coal; And
With the ratio Qs/Qc of the mass rate Qs of described water vapour and the mass rate Qc of described carbon reach more than 1.0 and the mass rate of 1.5 following modes, the mass rate of regulating the described coal that described coal nozzle supplied with and the described water vapour that described steam jet is supplied with at least one party's operation.
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| JP2010-095498 | 2010-04-16 | ||
| JP2010095498 | 2010-04-16 | ||
| PCT/JP2011/058711 WO2011129243A1 (en) | 2010-04-16 | 2011-04-06 | Operational method for coal gasification reaction furnace and coal gasification reaction furnace |
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| CN102884162B CN102884162B (en) | 2015-02-25 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104498075A (en) * | 2014-12-19 | 2015-04-08 | 中美新能源技术研发（山西）有限公司 | Quick hydropyrolysis reactor and process thereof |
| CN106590753A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Gasification device for preparing methane-rich synthesis gas by coal and method of gasification reaction |
| CN107429176A (en) * | 2015-05-22 | 2017-12-01 | 新日铁住金工程技术株式会社 | The method of operation of coal gasification systems |
| CN111511880A (en) * | 2017-12-26 | 2020-08-07 | 株式会社Posco | Attached mineral measuring device of coke bin |
| CN112831352A (en) * | 2021-01-09 | 2021-05-25 | 中国华能集团清洁能源技术研究院有限公司 | Efficient gasification furnace and working method thereof |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560204B (en) * | 2013-10-22 | 2017-05-17 | 任相坤 | Water coal slurry and natural gas combined gasification furnace with multiple nozzles |
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| JPS59140291A (en) * | 1983-02-01 | 1984-08-11 | Shinenerugii Sogo Kaihatsu Kiko | Gasification of pulverized coal under pressure |
| US20030130360A1 (en) * | 2001-03-06 | 2003-07-10 | Kindig James Kelly | Method for the production of hydrogen-containing gaseous mixtures |
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| JPH07331256A (en) * | 1994-06-15 | 1995-12-19 | Nippon Steel Corp | Method for operating rapid thermal cracking of coal |
| JP2004217868A (en) * | 2003-01-17 | 2004-08-05 | Nippon Steel Corp | Coal thermal hydrocracking process |
| JP4898759B2 (en) * | 2008-10-22 | 2012-03-21 | 三菱重工業株式会社 | Coal gasifier |
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- 2011-04-06 WO PCT/JP2011/058711 patent/WO2011129243A1/en active Application Filing
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59140291A (en) * | 1983-02-01 | 1984-08-11 | Shinenerugii Sogo Kaihatsu Kiko | Gasification of pulverized coal under pressure |
| US20030130360A1 (en) * | 2001-03-06 | 2003-07-10 | Kindig James Kelly | Method for the production of hydrogen-containing gaseous mixtures |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104498075A (en) * | 2014-12-19 | 2015-04-08 | 中美新能源技术研发（山西）有限公司 | Quick hydropyrolysis reactor and process thereof |
| CN107429176A (en) * | 2015-05-22 | 2017-12-01 | 新日铁住金工程技术株式会社 | The method of operation of coal gasification systems |
| CN106590753A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Gasification device for preparing methane-rich synthesis gas by coal and method of gasification reaction |
| CN106590753B (en) * | 2015-10-19 | 2020-09-04 | 中国石油化工股份有限公司 | Gasification device and method for preparing methane-rich synthesis gas from coal |
| CN111511880A (en) * | 2017-12-26 | 2020-08-07 | 株式会社Posco | Attached mineral measuring device of coke bin |
| CN112831352A (en) * | 2021-01-09 | 2021-05-25 | 中国华能集团清洁能源技术研究院有限公司 | Efficient gasification furnace and working method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102884162B (en) | 2015-02-25 |
| AU2011242111A1 (en) | 2012-12-06 |
| JP5386635B2 (en) | 2014-01-15 |
| JPWO2011129243A1 (en) | 2013-07-18 |
| WO2011129243A1 (en) | 2011-10-20 |
| AU2011242111B2 (en) | 2013-11-07 |
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