CN100447221C - Method and device for gasification - Google Patents
Method and device for gasification Download PDFInfo
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- CN100447221C CN100447221C CNB038036053A CN03803605A CN100447221C CN 100447221 C CN100447221 C CN 100447221C CN B038036053 A CNB038036053 A CN B038036053A CN 03803605 A CN03803605 A CN 03803605A CN 100447221 C CN100447221 C CN 100447221C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/095—Exhaust gas from an external process for purification
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Industrial Gases (AREA)
Abstract
A gasification device and a gasification method for solid fuel capable of lowering the temperature of generated gas discharged from a gasification furnace while increasing a fuel-to-gas conversion efficiency, the gasification device comprising a washer washing with water and collecting soot and dust including unreacted inflammable components accompanying the generated gas flowing through a regenerated gas flow passage, a dehydrator generating slurry by regulating the water amount of washing waste including soot and dust collected by the washer, a pump for pressurizing the produced slurry and transporting the slurry, and a nozzle installed at a step part where an upper stage burner is installed and feeding the slurry to the gasification furnace; the gasification method comprising the steps of allowing the slurry fed from the nozzle into the gasification furnace to be accompanied by a downward flow formed by the upper stage burner and flowing the slurry in a direction opposed to the flow of the regenerated gas in the gasification furnace led to an outlet.
Description
Technical field
The present invention relates to solid-fuelled gasification technology, relate in particular to method for solid fuels gasification and the system thereof that flushes a formula (flush-bedtype) gasifier that use.
Background technology
Various types of gasification systems have been proposed, comprise fixed-bed type, efflorescence bed formula (pulverizedbed type) and carry a formula (entrained bed type) secretly, wherein pulverized, utilize oxygen partly to burn, to produce gas such as solid fuels such as solid hydrocarbon coals.In all these systems, in being called as the system of carrying a formula secretly, can operate gasifier with higher relatively temperature (such as 1500 ℃), be converted into the gasifier height of the transformation efficiency of gas by fuel like this than other types.In addition, because gasifier can operate under higher relatively temperature, thus can be melted such as the ash in the solid fuels such as hydrocarbon polymer, thus ash can be recovered and be utilized again as slag.
Similarly flush in the gasification system of formula gasifier being equipped with above description, in gasifier, produce and be attended by dust from the gasifier expellant gas, contain the combustiblecomponents that is not transformed in these dust, for example carbon part (as carbon parts such as unconverted charcoal and tar).Thus, proposed some gasification systems, they are constructed like this: follow the combustiblecomponents of synthetic gas to be supplied to get back to gasifier, so that utilize combustiblecomponents best, and the transformation efficiency of raising from fuel to gas.For example, with reference to Japanese publication patent disclosure No.07-278575.
Disclosed gasification system is equipped with cylindrical gasifier in Japanese publication patent disclosure No.07-278575, on an end of cylindrical gasifier, syngas outlet is set, the burner that fuel and oxygen or air are provided is set on the other end of cylindrical gasifier.From synthetic gas, reclaim and follow dust the synthetic gas of discharging, that comprise the combustiblecomponents that is not transformed from the outlet of gasifier, and the dust that is recovered with mix such as solid fuels such as fine coal with the formation slurry.Utilize pump that described slurry is pressurized to more than the working pressure of gasifier then, and this slurry is supplied to get back to gasifier.
In traditional gasifier, for the gas cooling that will be produced in the gasifier is admitted to equipment wherein or installs under the required temperature to synthetic gas, a kind of water cooler is provided, described water cooler is included in the continuous synthesis gas passage in gasifier exit, so that the synthetic gas that cooling is discharged from gasifier.If synthetic gas will be handled by desulphurization system for example, synthetic gas must just be cooled to normal temps before desulfurization is handled so, because described processing is normally carried out at normal temperatures.As the above-mentioned vaporizer (boiler) that is used for cooling syngas, vaporizer formula water cooler is used, and comes synthetic gas is cooled off by the fluid class water of the passage of flowing through or the heat exchange between steam and the synthetic gas in described vaporizer formula water cooler.
In this heat exchange, depend on the temperature of the synthetic gas that gasifier discharges, when following the ash fusing of the synthetic gas of discharging from gasifier, can produce slag.If use water cooler as described below, promptly this water cooler be equipped in the synthetic gas passage and have a plurality of be used to make with synthetic gas carry out the pipe that the fluid of heat exchange flows through, slag may stick on the interval between the fluid hose so, and the possibility of result can stop up the synthetic gas passage.For to become the same high gasification system of temperature with the slag that is produced of the temperature of the synthetic gas of discharging from gasifier, in order to prevent that slag from stopping up passage, the water cooler that for example has water wall construction or shell type (jacket) structure is connected with the outlet of gasifier, and the described water cooler that has water wall construction or nested structure is such structure: the fluid channel that promptly is used for carrying out with synthetic gas heat exchange is installed in the wall that constitutes the synthetic gas passage.
Because above-mentioned heat exchanger effectiveness or the cooling efficiency that has the water cooler of water wall construction or nested structure is lower than the water cooler that constitutes by the inside that a plurality of pipes is installed in the synthetic gas passage, so the size of water cooler becomes very big.For example, might need tens meters high water coolers for several meters high gasifier.Make the size of gasification system become big, cost increase as the above-mentioned water cooler that has water wall construction or nested structure that is installed in the gasification system.Thus, need reduce to have the size of the water cooler of water wall construction or nested structure by the temperature that reduces the synthetic gas of discharging from gasifier.
In order to realize the above purpose, the slurry that dust produced that the present inventor's imagination will reclaim from the synthetic gas that gasifier is discharged is conducted to the syngas outlet of gasifier, utilizes the moisture evaporation of the slurry of the syngas outlet that is conducted to gasifier to reduce from the temperature of the synthetic gas of gasifier discharge then.Yet if slurry is conducted to the syngas outlet of gasifier, the slurry that is provided is accompanied by synthetic gas and discharges from gasifier so.The result, supplied back traditional gasification system of gasifier to compare with the slurry that comprises dust, being included in the hold-time that unconverted combustiblecomponents in the slurry remains in the gasifier shortens, therefore unconverted combustiblecomponents is not easy to react in gasifier, and the transformation efficiency from fuel to gas is difficult to improve.Be in above-mentioned reason, need to reduce temperature, improve the transformation efficiency from fuel to gas simultaneously from the synthetic gas of gasifier discharge.
Summary of the invention
The purpose of this invention is to provide a kind of energy and reduce gasification process and the gasification system that improves the transformation efficiency from fuel to gas from the temperature of the synthetic gas of gasifier discharge, simultaneously.
Gasification process of the present invention will be followed gas and comprise the slurry that the dust of unconverted combustiblecomponents produces and be conducted to syngas outlet by recovery, described gas produces and discharges from the exit of gasifier, described gasifier partly buring solid fuel produces synthetic gas, the described slurry that is supplied to along with flow towards the opposite direction of gasifier outlet mobile synthetic air.
By said structure,, therefore utilize the moisture content in the slurry can reduce from the temperature of the synthetic gas of gasifier discharge because slurry is conducted to the syngas outlet of gasifier.In addition, since the slurry that infeeds gasifier along with flow towards the opposite direction of outlet mobile synthetic air, therefore being included in the time that the unconverted composition in the slurry keeps in gasifier can be longer, thereby can increase the reacting weight that is included in the combustiblecomponents in the slurry.Thus, the temperature of the synthetic gas of discharging from gasifier can reduce, and can improve the transformation efficiency from fuel to gas simultaneously.
In addition, described gasifier comprises burner and last burner down, described burner down infeeds gasifier with solid fuel, the described burner of going up is installed than the more close described outlet of the following burner of gasifier, and not only solid fuel is infeeded in the gasifier, and in gasifier, forming downward flowing, described slurry is conducted in the level (stage) that burner on the gasifier is installed.By this structure follow downward the flowing that forms by last burner owing to be conducted to the slurry of gasifier outlet, so slurry can be easily in gasifier inside along with towards exporting the opposite reversed flow of mobile synthetic air.
In addition, if described slurry ejection also enters in the gasifier, so that along with in gasifier, form to flow in the opposite direction towards the synthetic air side of outlet, even not have to form any mobile along with towards the opposite direction of outlet mobile synthetic air in that gasifier is inner so, such as flowing downward of forming by last burner, described slurry also can along with flow towards the opposite direction of outlet mobile synthetic air.
In addition, gasification system of the present invention comprises: the gasifier that produces gas by the partial combustion solid fuel; The synthetic gas passage, the gas that produces in gasifier is by described synthetic gas channel flow; Be installed in the slurry generation device in the synthetic gas passage, be used to reclaim and follow synthetic gas and dust that contain unconverted combustiblecomponents, and produce slurry by the dust that reclaims; Pump is used for the slurry that described slurry generation device is produced is pressurizeed and transmits described slurry; And nozzle, described nozzle will infeed the gasifier from the slurry that the slurry generation device transmits by pump; Nozzle is installed in the syngas outlet place of gasifier, and the slurry that infeeds gasifier from nozzle along with gasifier, flow in the opposite direction towards outlet mobile synthetic air side.
Utilize said structure,, therefore utilize the moisture content in the slurry can reduce from the temperature of the synthetic gas of gasifier discharge because slurry is conducted to the syngas outlet of gasifier.In addition, since the slurry that infeeds gasifier from nozzle along with flow in the opposite direction towards outlet mobile synthetic air side, therefore being included in the time that the unconverted combustiblecomponents in the slurry keeps in gasifier can be longer, and the reacting weight that is included in the combustiblecomponents in the slurry thus can increase.Thus, the temperature of the synthetic gas of discharging from gasifier can reduce, and can improve the transformation efficiency from fuel to gas simultaneously.
In addition, described gasifier comprises burner and last burner down, described burner down infeeds gasifier with solid fuel, the described burner of going up is installed as than the more close described outlet of the following burner of gasifier, and not only solid fuel is infeeded in the gasifier, and in gasifier, forming downward flowing, described nozzle is installed in the level that burner on the gasifier is installed.The said structure of the two-stage combustion device formula gasifier by being equipped with burner and following burner, wherein nozzle is installed in the level that burner is installed, owing to follow by flowing downward that last burner forms from the slurry that nozzle infeeds gasifier, thus slurry can be easily along with mobile in gasifier in the opposite direction towards outlet mobile synthetic air side.
In addition, described slurry generation device comprises: washer, described washer utilize water or alkaline solution washing mobile synthetic gas in the synthetic gas passage, to remove and to reclaim the dust of following synthetic gas from synthetic gas; And water trap, being used for removing portion water to regulate the moisture content of slurry from washer sewage, wherein said washer sewage contains the dust that is reclaimed by washer.Said structure is preferred, because contain in the process of slurry of dust in generation, unnecessary installation is used for water is added to any device of dust.
In addition, described system equipment has Temperature Detector, is used to measure the temperature from the synthetic gas of gasifier discharge, and wherein said slurry generation device is adjusted the moisture content of slurry according to the synthetic gas temperature that Temperature Detector detected.Said structure is preferred, because can control the temperature of the synthetic gas of discharging according to the moisture content in the slurry from gasifier.
In addition, the present invention is a kind of hydrogen production system, is equipped with according to the described gasification system of either side in the above-mentioned aspect, and wherein solid fuel is the solid carbon hydrogen compound.In addition, the present invention is a kind of hydrogen production system, be equipped with according to each described gasification system and catalyst converter in the above-mentioned aspect, described catalyst converter comprises the catalyzer that is used for from the reaction of carbon monoxide and water generates hydrogen, described carbon monoxide is included in the synthetic gas of discharging from gasification system, and wherein said solid fuel is the solid carbon hydrogen compound.Hydrogen production system with said structure can not only increase the hydrogen density in the synthetic gas, and size can be made lessly.
Description of drawings
Fig. 1 shows the brief configuration of the gasification system of using embodiments of the invention 1 and the sketch of operation;
Fig. 2 shows the brief configuration of the gasifier in the gasification system that is installed in embodiment 1 and the vertical sectional view of operation;
Fig. 3 is the horizontal cross of level (stage) that burner is installed down, shows the brief configuration and the operation of gasifier in the gasification system that is installed in embodiment 1;
Fig. 4 is the horizontal cross that the level of burner is installed, and shows the brief configuration and the operation of the gasifier in the gasification system that is installed in embodiment 1;
Fig. 5 shows the brief configuration of the gasification system of using embodiments of the invention 2 and the sketch of operation;
Fig. 6 shows the brief configuration of the gasification system of using embodiments of the invention 3 and the sketch of operation;
Fig. 7 shows the brief configuration of the embodiment that is equipped with the hydrogen production system of using gasification system of the present invention and the sketch of operation.
Embodiment
(embodiment 1)
To use Fig. 1 to 4 to describe gasification system of the present invention below.Fig. 1 shows the brief configuration of application gasification system of the present invention and the sketch of operation.Fig. 2 shows and is installed in the brief configuration of using the gasifier in the gasification system of the present invention and the vertical sectional view of operation.Fig. 3 is the horizontal cross that the level of burner is installed down, shows to be installed in the brief configuration and the operation of using the gasifier in the gasification system of the present invention.Fig. 4 is the horizontal cross that the level of burner is installed, and shows to be installed in the brief configuration and the operation of using the gasifier in the gasification system of the present invention.The gasification system that is equipped with spiral streaming gasifier (spiral flow type gasifier) has been described in this embodiment, wherein burner is installed in two different level places: go up burner and be used to form elevating screw stream, and burner is used to form the decline helical flow down.
As shown in Figure 1, the gasification system of this embodiment comprises: gasifier, and this gasifier is to gasifying as solid-fuelled granular or powdery solid hydrocarbon polymer (such as fine coal); Gas scrubber 3 is removed the dust of carbon containing part (being unconverted combustiblecomponents) in the gas of this gas scrubber water or alkaline solution washing and generation from gasifier 1; Water trap 5 is isolated a part of water in that this water trap is discharged, as to contain charcoal (char) the washer sewage from gas scrubber; Thick fluid pump 7, this thick fluid pump pressurizes to the slurry that produces by adjustment moisture content in water trap 5 and transmits described slurry; Washing water pump 9, described pump turns back to washer 3 with dehydrated device 5 isolating water; And nozzle 11, described nozzle 11 infeeds the slurry that thick fluid pump 7 transmits in the gasifier 1.
As shown in Figure 3, following burner 21 is installed into: with tangential direction contact circle 27, wherein round 27 is concentric and suppose that this circle 27 is positioned in the position of helical flow with generation with the outer side wall of gasifier 1 from the fuel injection direction of lower combustion chamber 21 ejection.By burner 21 down is installed as mentioned above, be created in the inside of the vaporizer 13 of gasifier 1 along the helical flow of concentric(al) circles 27.In this embodiment, four burners 21 are installed with the interval that equates.As shown in Figure 4, last burner 25 is installed into: with tangential direction contact circle 29, wherein said circle 29 is concentric and suppose that this circle 29 is positioned in the position of helical flow with generation with the outer side wall of gasifier 1 from the fuel injection direction of upper combustion chamber 25 ejection.By installing burner 25 as mentioned above, be created in the inside of the vaporizer 13 of gasifier 1 along the helical flow of concentric(al) circles 29.In this embodiment, go up the interval installation of burner 25 for two to equate.
In this embodiment, nozzle 11 as above burner 25 is equally installed, and its direction is with tangent line contact circle 29, and wherein said circle 29 is concentric and suppose that this circle 29 is positioned in the position of helical flow with generation with the outer side wall of gasifier 1.In this embodiment, two nozzles 11 alternately are installed in equal interval but with last burner 25 and go up the level place that burner 25 is mounted in the gasifier 1.In this structure, nozzle 11 is not must be installed on the height that equates with last burner 25, can be installed in than on the high or low position of last burner 25, go up the same stages place that burner 25 is mounted in the gasifier 1 as long as it is installed in, the slurry of supplying with from nozzle can be followed the helical flow that is formed by last burner 25 thus.
In addition, as in the present embodiment, burner 25 is in the gasifier 1 of two-stage combustion device on gasifier 1, the slurry that infeeds gasifier 1 from nozzle 11 is accompanied by the decline helical flow that burner 25 forms, promptly flow downward, therefore flow the outlet 23 of synthetic air in gasifier 1 along the direction opposite with upwelling.Thus, nozzle 11 does not need to be mounted as in the present embodiment the helical flow that is used for forming along concentric(al) circles 29.Yet preferably, as in the present embodiment, nozzle 11 is mounted the helical flow that is used for forming along concentric(al) circles 29, because the decline helical flow that is formed by last burner 25 is difficult to by disturbance.
Before fine coal (pre-pulverized coal) be divided into down fuel tube 31, be connected to down burner 21 and last fuel tube 33 the solid fuel passage, be connected to the solid fuel passage of burner 25, as illustrated in fig. 1 and 2, and by down burner 21 and last burner 25 with infeeding in the gasifier 1 such as non-combustible gas such as nitrogen and carbonic acid gas.In addition, following oxygen hose 35 and last oxygen hose 37 are connected to down burner 21 and last burner 25 respectively, wherein each oxygen hose is oxygen or air passageways, be used for causing down burner 21 and last burner 25 as the oxygen of vaporized chemical, oxygen or air are by burner 21 and last burner 25 infeed in the gasifier 1 with fine coal down.
The gas that produces in the vaporizer 13 of gasifier 1 is introduced into syngas tube 59, this syngas tube 59 is synthetic gas passages, and under the situation that water cooler 17 is not installed, be connected to the outlet 23 of the vaporizer 13 of gasifier 1, perhaps under the situation that water cooler 17 is installed, be connected to the upper end of water cooler 17.The synthetic gas that enters in the syngas tube 59 passes through syngas tube 59, is introduced into the gas scrubber 3 that is connected with syngas tube 59, as shown in Figure 1.
Be introduced into by Purge gas pipe 61 as the Purge gas of the synthetic gas that had been cleaned by gas scrubber 3 and be arranged in other equipment after the gasification system and install, wherein said Purge gas pipe 61 is the Purge gas passages that are connected with gas scrubber 3.On the other hand, from gas scrubber 3, comprise the washer sewage that is accompanied by synthetic gas and be introduced into water trap 5 by washer waste pipe 63 such as dust such as charcoals, wherein said washer waste pipe 63 is passages of washer sewage.Like this, be independent of water cooler 17, the water cooler that is used for cooling and purifying gas can be installed in Purge gas pipe 61 according to the temperature of the Purge gas that flows through Purge gas pipe 61 or other equipment and the needed Purge gas temperature of device that are installed in after the gasification system.The water cooler of installing for Purge gas pipe 61 generally includes a plurality of pipes, is used for cooling off the medium of the passage that is installed in Purge gas.Water trap 5 is separated superfluous water and the washer sewage of introducing from gas scrubber 3 by washer waste pipe 63, and produces the slurry that comprises charcoal.It can be applicable to the above water trap 5 in using and to be any type in filter screen, strainer, sedimentation basin and the whizzer, as long as can separate the water of surplus from washer sewage.As mentioned above, gas scrubber 3 and water trap 5 constitute the slurry generation device.
Below description is had the operation of the gasification system of said structure of the present invention and feature.The down level place of burner 21 is installed in gasifier 1, the partial oxidation of combustiblecomponents in the solid fuel under the help of vaporized chemical, i.e. the partial combustion of the combustiblecomponents in solid fuel makes that the temperature at this place is very high, such as up to 1500 ℃.Utilization is at the described high temperature of vaporizer 13 inside, and the ash in the solid fuel is melted, and is recycled in the slag recovery chamber 15 by slag notch 39.
On the other hand, the residue combustiblecomponents in solid fuel is converted to inflammable gas in vaporizer 13, such as hydrogen and carbon monoxide.The inflammable gas that produces in vaporizer 13 is drained into the syngas tube 59 from the outlet 23 of gasifier 1.Comprise as carbon part of unconverted combustiblecomponents and follow synthetic gas flows through syngas tube 59 from gasifier 1 dust under the help of washing water, to be reclaimed by gas scrubber 3.When the water that makes predetermined amount by water trap 5 from from gas scrubber 3, comprise when separating the washer sewage that is recovered dust, washer sewage is made with the slurry of desired density.
Utilize thick fluid pump that the slurry that is obtained is pressurized on the working pressure of gasifier 1, and it is infeeded the gasifier from nozzle 11.The slurry that infeeds in the gasifier 1 is followed downward flowing, described downward mobile by last burner 25 forms, in gasifier 1 inside along with towards the flowing of the opposite direction of the outlet 23 mobile synthetic gas of gasifier 1, and described slurry flow in the gasifier 1 that burner 21 down is mounted grade in.When the unconverted combustiblecomponents as slurry is moved down into from nozzle 11 level of burner 21 under the installation in the gasifier 1 for getting back to, when being moved upwards up to the level of installing burner 25 then from the level that burner 21 is installed down, they are exposed reacts and gasification once more.Therefore in addition, because aqueous slurry is conducted to the level of installing burner 25 from nozzle 11, be cooled so the water in slurry, is installed the level of burner 25 thus by the heat of vaporization in the gasifier 1, the temperature of the synthetic gas of discharging from gasifier is lowered.
Now, in the gasification system of the spiral streaming gasifier that is equipped with band two-stage combustion device, the gasification system of traditional gasification system and present embodiment is compared, comparison is from the temperature out of the synthetic gas of gasifier and the transformation efficiency from fuel to gas, wherein be supplied to the level place of burner under the installation at slurry described in described traditional gasification system, result relatively is as shown in table 1.Transformation efficiency means the transformation efficiency from the raw material calorific value to the synthetic gas calorific value, and is as follows:
(transformation efficiency)=(synthetic gas calorific value)/(fuel value) * 100
Table 1
As shown in table 1, in traditional gasification system, because under oxygen/coal weight ratio was 0.8 situation, for the influence of moisture content in the slurry, the gasifier internal temperature was 1300 ℃, so the ash in the raw material can not melt.Because the gasifier internal temperature is 1300 ℃ a lesser temps, so transformation efficiency is also low, is 55%.So, increase as the supply of the oxygen of vaporized chemical, make oxygen/coal weight ratio reach 1.0, thereby make the gasifier internal temperature be increased to about 1500 ℃, ash can melt, and transformation efficiency is increased to 60%.Yet, be increased to about 1200 ℃ from the temperature out of the synthetic gas of gasifier, and follow the ash semi-molten of synthetic gas thus, and adhere to the outlet of gasifier.
On the other hand, in the gasification system of present embodiment, be that the gasifier internal temperature can be increased to about 1500 ℃, so ash can melt under 1.0 the situation in oxygen/coal weight ratio.In addition, can be cooled to about 900 ℃, therefore can prevent that ash from adhering to the outlet of gasifier from the temperature out of the synthetic gas of gasifier.In addition, transformation efficiency remains on 60%, and can not reduce.
In the gasification system of present embodiment, when the level that burner is mounted on slurry is conducted in gasifier is located, promptly be conducted to syngas outlet 23 1 sides of gasifier, and the moisture content in the slurry be equipped with gasifier 1 under the heat effect of level of burner 25 when being evaporated, the level that the last burner 25 of gasifier 1 is installed is cooled, and the temperature of the synthetic gas of discharging from gasifier 1 can be lowered, as mentioned above.In addition, when flow in the opposite direction with the synthetic air side of gasifier 1 inside that flows to outlet 23 in the slurry edge that infeeds gasifier 1 from nozzle 11, the retention time of unconverted combustiblecomponents in gasifier 1 that is contained in the slurry can be elongated, and the reacting weight that therefore is contained in the unconverted combustiblecomponents in the slurry can increase.Thus, the temperature of the synthetic gas of discharging from gasifier can reduce, and can improve the transformation efficiency from fuel to gas simultaneously.
In addition, in the gasification system of present embodiment, because the temperature of the synthetic gas of discharging from gasifier can be lowered, and required thus cooling power can be lowered, therefore be connected to the size of the water cooler of gasifier outlet, all water coolers 17 as shown in Figure 2, can be manufactured less.In addition, if the temperature of the synthetic gas of discharging from gasifier is less than the temperature that may produce slag, can replace water cooler 17 shown in Figure 2 with water cooler as described below so, described water cooler comprises a plurality of pipes that are used for cooling off the medium that is contained in the gas passage and has the cooling efficiency higher than water cooler 17, thereby the size of water cooler can be made very for a short time.In addition, although water cooler set up the temperature that depends on by the supply of slurry institute refrigerative synthetic gas, yet be connected to the water cooler of gasifier outlet, water cooler 17 for example shown in Figure 2 can be omitted.Be connected to the result of the water cooler of gasifier outlet as omission, it is less that the size of gasification system can be made, and become instinct to reduce.
Especially, although the picture spiral streaming gasifier that has the two-stage combustion device in the present embodiment can flush an efficient of formula gasifier and gasifies to be higher than other, and furnace volume can be very little when comparing under the same treatment ability, but because high heat load, the temperature of the synthetic gas of discharging from gasifier is higher than other and flushes a formula gasifier.Thus, for the gasification system that is equipped with spiral streaming gasifier in the similar present embodiment, the water cooler size that is connected to gasifier outlet of similar water cooler 17 becomes big, and result's size of gasification system in many cases becomes big, cost and increases.Consider above situation, the present invention is applied in the gasification system of spiral streaming gasifier of the band two-stage combustion device that is equipped with similar present embodiment, flush a gasification system of formula gasifier and compare with being equipped with other like this, can aspect the reducing of the size of gasification system and cost, produce bigger effect.Yet, the present invention not only can be applied to equip in the gasification system of spiral streaming gasifier, and can be applied to equip a various gasification system of formula gasifier that flush, comprise the gasification system of having equipped other, have the two-stage combustion device or only have the gasifier of one-level burner.
In addition, because the gas scrubber 3 and the water trap 5 that utilize washing water to reclaim dust from synthetic gas in the present embodiment are used as the slurry generation device, therefore for the generation of the slurry that contains dust, do not need to install any device that is used for water is added to the dust that is recovered with drying regime.Yet the present invention also can be constructed to: utilize cyclonic separator to reclaim dust with drying regime from synthetic gas, and produce slurry by water is added in the described dust.
In addition because in the gasification system of present embodiment, dust pressurized and as slurry by for getting back in the gasifier, therefore the dust under the drying regime is compared for the system of getting back to gasifier with utilizing false-bottom bucket, do not need to be used for the nitrogen that dust transmits.Thus, not planning the density of from synthetic gas collected other gases (such as the nitrogen in the synthetic gas) can be lower, and wants the density of collected gas can be higher.For example, collect hydrogen if plan to utilize as solid-fuelled hydrocarbon polymer, the hydrogen density in the synthetic gas can be higher so.In addition, owing to do not use false-bottom bucket, the one-tenth instinct of false-bottom bucket is saved.In addition, as shown in table 1, the transformation efficiency from the solid fuel to the synthetic gas can increase.
In addition, go up burner 25 and two nozzles 11 though equipped four following burners 21, two among this embodiment, yet the quantity of following burner and last burner can be selected as required, burner 21 and last burner 25 can form helical flow under needing only, the quantity of the nozzle 11 of present embodiment also can be selected according to the ability of nozzle as required, as long as they are used for slurry is infeeded the purpose of gasifier 1.Yet, preferably, the nozzle 11 of abundant amount is installed in position, so that the decline helical flow that is formed by last burner 25 is not easy by disturbance.
(embodiment 2)
Fig. 5 shows the brief configuration of application gasification system of the present invention and the sketch of operation.In this embodiment, give same parts or mechanism with label identical among the embodiment 1, and further do not describe.Following description covers structure and the feature that is different from embodiment 1.
The difference of the gasification system of present embodiment and embodiment 1 is: the temperature of the synthetic gas of discharging from gasifier is detected, and the moisture content in the slurry is conditioned according to temperature.The gasification system of present embodiment is equipped with: thermometer 69 is used for detecting the temperature of the synthetic gas that flows through syngas tube 59; And controller 71, being used for controlling the operation of water trap 5, thermometer 69 and controller 71 are installed in the part that is connected to gasifier 1 outlet of syngas tube, as shown in Figure 5.Thermometer 69 is electrically connected to controller 71 by distribution 73, and controller 71 is electrically connected to water trap 5 by distribution 73.
Cool off and the temperature of the synthetic gas of discharging from gasifier depends on the ratio of dust and water the slurry by the supply of slurry.Therefore, in the gasification system of present embodiment, thermometer 69 is measured from the temperature of the synthetic gas of gasifier 1 discharge, and is sent to controller 71 with the corresponding temperature signal of described measurement.Temperature and the preset temperature or the temperature range of the synthetic gas of discharging from gasifier 1 that utilizes that thermometer 69 measures, having received controller from the temperature signal of thermometer 69 calculates and will infeed the water-mass density of the slurry the gasifier 1 from nozzle 11, the operation of control water trap 5, and adjust and will carry out isolating moisture content by water trap 5.Thus, the slurry that has been conditioned when wherein moisture content infeeds the gasifier 1 from nozzle 11, and the temperature Be Controlled of the synthetic gas of discharging from gasifier 1 keeps constant.
In the gasification system of present embodiment, as mentioned above, be conducted to the outlet of gasifier 1 by the slurry that wherein moisture content has been conditioned according to the temperature of the synthetic gas of discharging from gasifier 1, the temperature of the synthetic gas of discharging from gasifier is controlled.
Because as previously mentioned, cool off and the temperature of the synthetic gas of discharging from gasifier depends on the ratio of dust and water the slurry by the supply of slurry, therefore if follow the Dust Capacity of synthetic gas to change, the temperature of the synthetic gas of discharging from gasifier also changes so.Thus, if follow synthetic gas dust amount in allowed limits, it is feasible adopting the structure of separating the water of constant basis from the washing water that comprise dust in embodiment 1.Yet, if follow the variation of amount of the dust of synthetic gas to exceed the scope that allows, the gasification system of so preferred utilization structure such as present embodiment.
(embodiment 3)
Fig. 6 shows the brief configuration of application gasification system of the present invention and the sketch of operation.In this embodiment, give same parts or mechanism with label identical among embodiment 1 and the embodiment 2, and further do not describe.Following description covers structure and the feature that is different from embodiment 1 and embodiment 2.
The difference of the gasification system of present embodiment and embodiment 1 and embodiment 2 is: the described system equipment formula gasifier that flows downward, the burner that is used to supply with solid fuel and vaporized chemical in this gasifier is installed in the top of gasifier, from the overhead stream to the bottom, syngas outlet is positioned at the place, bottom of gasifier to the gas that produces in gasifier in gasifier.In brief, the gasification system of present embodiment is equipped with gasifier 75, and syngas tube 59 is connected to the outlet that is positioned at place, gasifier 75 bottoms, and burner 79 is installed in the top of gasifier 75, and nozzle 11 is installed in the bottom, that is, and and the exit of gasifier 75.
Infeed in the gasifier 75 by fuel feed pipe 81, the fuel channel that is connected to burner 79 and burner 79 as fine coal before solid-fuelled.Simultaneously, the oxygen as vaporized chemical infeeds in the gasifier 75 by oxygen supply-pipe 83, the oxygen that is connected to burner 79 or air passageways and burner 79.When the part of the combustiblecomponents in the solid fuel when oxidized, produces very high temperature by vaporized chemical in gasifier 75, for example about 1500 ℃, and the remainder of above-mentioned combustiblecomponents is converted to inflammable gas, such as hydrogen and carbon monoxide.Take out synthetic gas by the composite tube 59 that is connected to the outlet that is positioned at place, gasifier 75 bottoms.
The slurry that comprises the dust that contains combustiblecomponents is by being generated the processing from the washer sewage of gas scrubber 3 in water trap 5, described slurry is pressurized to by thick fluid pump 7 on the working pressure of gasifier 75, infeeds the bottom of gasifier 75 then by nozzle 11.The nozzle 11 of present embodiment is installed like this so that slurry upwards sprays and sprays in the gasifier 75, thus from the slurry of nozzle 11 ejection gasifier 75 along synthetic gas upward to injection.Thus, the slurry that infeeds gasifier 5 from nozzle 11 along with flow towards the opposite direction of the outlet mobile synthetic air of gasifier 75.By this structure, the slurry that infeeds gasifier 75 from nozzle 11 is exposed on the following long period of high temperature of gasifier 75 inside, and unconverted combustiblecomponents reacts in slurry thus, produces inflammable gas, such as carbon monoxide etc.In addition, infeed moisture content evaporation immediately after infeeding gasifier 75 slurry of gasifier 75, and the bottom of gasifier 75 from nozzle 11, thus the temperature of the synthetic gas that cooling is discharged from gasifier 75.
According to present embodiment, the temperature of the synthetic gas of discharging from gasifier can reduce, and improves the transformation efficiency from fuel to gas simultaneously, as mentioned above.Thus, present embodiment not only can be applied to following gasification system, described gasification system be equipped with the spiral streaming gasifier of band two-stage combustion device or described in embodiment 1 and embodiment 2 wherein synthetic gas flow to the gasifier at top from the bottom, and except that above-mentioned gasification system, can also be applied to be equipped with a various gasification system of formula gasifier that flush, as long as flow into the gasifier along the direction opposite with the synthetic air that exports towards gasifier from the slurry of nozzle ejection.
(embodiment 4)
Fig. 7 shows the brief configuration of the embodiment that is equipped with the hydrogen production system of using gasification system of the present invention and the sketch of operation.In this embodiment, give same parts or mechanism with label identical in embodiment 1,2 and 3, and further do not describe.Following description covers structure and the feature that is different from embodiment 1,2 and 3.
Present embodiment is to use the hydrogen production system of the gasification system among the embodiment 1.The hydrogen production system utilization of present embodiment is by granular or powdery solid hydrocarbon polymer, makes hydrogen such as the material that fine coal etc. is made, and described hydrogen production system comprises: the similar gasifier 1 of the gasification system among structure and the embodiment 1; Gas scrubber 3; Water trap 5; Thick fluid pump 7; Washing water pump 9; And be installed in nozzle 11 on the gasifier 1, and and also have: following raw material hopper 85, it is connected to down burner 21 by fuel tube 31 down; Last raw material hopper 87, it is connected to burner 25 by last fuel tube 33; And shift converter (shift convert) 89, it is installed on the Purge gas pipe 61 and comprises catalyzer.
Be divided into two parts as the preceding fine coal of making the raw material that hydrogen uses, two portions corresponding respectively raw material hopper 85 and last raw material hopper 87 down, and be stored in down respectively in raw material hopper 85 and the last raw material hopper 87.The raw material that is stored in down in raw material hopper 85 and the last raw material hopper 87 is discharged from following raw material hopper 85 and last raw material hopper 87 with specified quantitative respectively, transmit the transmission nitrogen mixing that nitrogen pipe 93 is supplied with transmit nitrogen pipe 91 and last raw material from the following raw material that is connected with the raw material relief outlet of following raw material hopper 85 and last raw material hopper 87 respectively then, and under air effect, be transmitted.Raw material and transmission nitrogen are conducted to down burner 21 by following fuel tube 31, and are conducted to burner 25 by last fuel tube 33, then from burner 21 and last burner 25 infeed the gasifier 1 down.In this operation, because oxygen or air are also respectively from oxygen hose 35 and last oxygen hose 37 are conducted to down burner 21 and last burner 25 down, therefore burner 21 and last burner 25 not only infeed raw material in the gasifier 1 down, and oxygen or the air as vaporized chemical infeeded in the gasifier 1.
Raw material and oxygen mix in gasifier 1, and the part of the combustiblecomponents in the raw material is oxidized, and produce very high temperature.The remainder of combustiblecomponents is converted to the gas that mainly comprises hydrogen and carbon monoxide, and synthetic gas takes out inflow syngas tube 59 from producer 1.Be washed in gas scrubber 3 when removing with the dust that will follow it at the synthetic gas of the syngas tube 59 of flowing through, the temperature of synthetic gas is higher than 100 ℃, and the part of washing water is evaporated and sneaks in the Purge gas under this heat effect thus.The Purge gas that has from gas scrubber 3 steam that obtains flows in the Purge gas pipe 61, and is introduced into 89 li of the shift converters that are installed in the Purge gas pipe 61.Shift converter 89 comprises known catalyst for water-gas shift reaction, and such as copper-plumbous formula catalyzer or iron-chromium formula catalyzer, they demonstrate the catalytic effect that quickens conversion shown in the formula (1).
CO+H
2O → CO
2+ H
2Formula (1)
Change in the stove 89 when vapoury Purge gas flows into, and during the contact transformation catalyzer, cause the conversion in the formula (1), the hydrogen density in purifying air with increase.Then, will purify air and from shift converter 89, take out, and it be delivered in other equipment and device that use product gas by Purge gas pipe 61 as product gas.As mentioned above, evaporation and sneak into part washing water in the Purge gas with the form of steam and be used as the required water of conversion in the shift converter 89 in gas scrubber 3.
On the other hand, the dust that the synthetic gas from gas scrubber 3 reclaims mixes with washing water, and is sent and enters in the washing pipe 63 as washer sewage.The washer sewage that enters in the washer waste pipe 63 is introduced in the water trap 5, and forms slurry after part moisture content is removed.Then, the slurry that refines in water trap 5 is forced into by thick fluid pump 7 on the working pressure of gasifier 1, is sent to nozzle 11 by slurry supply-pipe 67 then, and infeeds the gasifier 1 from nozzle 11.Unconverted carbon part in the slurry in infeeding gasifier 1 is further reacted in gasifier 1, and changes into such as gases such as carbon monoxide.The step that burner 25 is mounted in the moisture content gasifier 1 in the slurry in infeeding gasifier 1, and in addition, described moisture content also is used for the conversion of formula (1) and converts hydrogen to.
In the hydrogen production system of present embodiment, wherein follow the dust of Purge gas to be supplied to be back to the outlet of gasifier as slurry, under the help of the water that infeeds the appropriate amount in the gasifier as slurry, the hydrogen density that carbon monoxide converts in hydrogen and the synthetic gas increases, as mentioned above then.In addition, aspect size, can make lessly or can remove owing to be connected to the water cooler of gasifier outlet, so the size of hydrogen production system can be made lessly.
In the hydrogen production system of present embodiment, when utilizing washing water to wash synthetic gas in gas scrubber 3, the part washing water are evaporated, and the washing water of evaporation are followed the Purge gas from gas scrubber.Contain in the shift converter 89 of transformation catalyst by being introduced by the Purge gas of stream trace, the remaining carbon monoxide in Purge gas can convert hydrogen to.Thus, the hydrogen density in product gas can further increase.In addition, because the required steam of conversion can return and wash evaporation of water by the confession of washing water and constitute, what therefore do not need to install other is used to supply with the evaporation of water device.In addition, when synthetic gas was cooled in gas scrubber 3, the heat of synthetic gas was utilized to produce steam, and described steam will be used for the conversion that shift converter 89 is taken place, and promptly gas directly contacts washing water, with the evaporation washing water.By this structure, and other vaporizer to be installed and to be utilized the heat of synthetic gas to compare by the structure that described vaporizer produces steam, the reduction of thermo-efficiency is minimized or is zero.
This embodiment can not only be applied to according to the gasification system of embodiment 1 to 3 and according to the hydrogen production system of embodiment 4, and can be applied to be equipped with gasification system with different structure and the hydrogen production system that flushes a formula gasifier.
Commercial Application
According to the present invention, a kind of gasification process and gasification system are provided, it can reduce from gasifier discharges The temperature of synthesis gas, improve simultaneously the conversion efficiency from fuel to gas.
Claims (10)
1. gasification process, wherein follow gas and comprise the slurry that the dust of unconverted combustiblecomponents produces and be conducted to syngas outlet by recovery, described gas produces and is discharged from from the exit of the gasifier that produces gas by buring solid fuel partly, the described slurry that is supplied to along with flow in the opposite direction towards the synthetic air side of gasifier outlet.
2. gasification process according to claim 1, wherein said gasifier comprises burner and last burner down, described burner down infeeds gasifier with solid fuel, the described burner of going up is installed than the more close described outlet of the following burner of gasifier, and not only solid fuel is infeeded in the gasifier, and in gasifier, forming downward flowing, described slurry is conducted to the level that burner on the gasifier is installed.
3. gasification process according to claim 1, the ejection of wherein said slurry also enters in the gasifier, so that flow along forming in gasifier in the opposite direction with synthetic air side towards outlet.
4. a gasification system comprises: the gasifier that produces gas by the partial combustion solid fuel; The synthetic gas passage, the gas that produces in gasifier is by described synthetic gas channel flow; Be installed in the slurry generation device in the synthetic gas passage, be used to reclaim and follow synthetic gas and dust that contain unconverted combustiblecomponents, and produce slurry by the dust that reclaims; Pump is used for the slurry that described slurry generation device is produced is pressurizeed and transmits described slurry; And nozzle, described nozzle will infeed the gasifier from the slurry that the slurry generation device transmits by pump; Wherein
Nozzle is installed in the syngas outlet place of gasifier, and the slurry that infeeds gasifier from nozzle along with gasifier, flow in the opposite direction towards the synthetic air side of outlet.
5. gasification system according to claim 4, wherein said gasifier comprises burner and last burner down, described burner down infeeds gasifier with solid fuel, the described burner of going up is installed than the more close described outlet of the following burner of gasifier, and not only solid fuel is infeeded in the gasifier, and in gasifier, forming downward flowing, described nozzle is installed in the level place that burner on the gasifier is installed.
6. gasification system according to claim 4, wherein said nozzle ejection slurry also enters in the gasifier slurry, so that flow along forming in gasifier in the opposite direction with synthetic air side towards outlet.
7. gasification system according to claim 4, wherein said slurry generation device comprises: washer, described washer utilizes water or alkaline solution washing mobile synthetic gas in the synthetic gas passage, so that remove and reclaim the dust of following synthetic gas from synthetic gas; And water trap, being used for removing portion water to regulate the moisture content of slurry from washer sewage, wherein said washer sewage contains the dust that is reclaimed by washer.
8. gasification system according to claim 4, wherein said system equipment has Temperature Detector, be used to measure the temperature from the synthetic gas of gasifier discharge, wherein said slurry generation device is adjusted the moisture content of slurry according to the synthetic gas temperature that Temperature Detector detected.
9. a hydrogen production system is equipped with gasification system according to claim 4, and wherein solid fuel is the solid carbon hydrogen compound.
10. hydrogen production system according to claim 9, wherein, described hydrogen production system also is equipped with catalyst converter, and described catalyst converter comprises the catalyzer that is used for by the reaction of carbon monoxide and water generates hydrogen, and described carbon monoxide is included in from the synthetic gas that gasification system is discharged.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP34173/2002 | 2002-02-12 | ||
| JP2002034173A JP4085239B2 (en) | 2002-02-12 | 2002-02-12 | Gasification method and gasification apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1630701A CN1630701A (en) | 2005-06-22 |
| CN100447221C true CN100447221C (en) | 2008-12-31 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB038036053A Expired - Fee Related CN100447221C (en) | 2002-02-12 | 2003-02-06 | Method and device for gasification |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP4085239B2 (en) |
| CN (1) | CN100447221C (en) |
| AU (1) | AU2003207084A1 (en) |
| WO (1) | WO2003068894A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP4490300B2 (en) * | 2005-02-04 | 2010-06-23 | 株式会社日立製作所 | Solid fuel gasifier and gasification method |
| DE102005035921B4 (en) * | 2005-07-28 | 2008-07-10 | Choren Industries Gmbh | Process for the endothermic gasification of carbon |
| JP2008231294A (en) * | 2007-03-22 | 2008-10-02 | Electric Power Dev Co Ltd | Two-stage gasification furnace |
| US7993131B2 (en) * | 2007-08-28 | 2011-08-09 | Conocophillips Company | Burner nozzle |
| AU2011241999B2 (en) * | 2010-04-16 | 2013-12-19 | Nippon Steel & Sumikin Engineering Co., Ltd. | Coal gasifier |
| EP3305876B1 (en) * | 2016-10-07 | 2019-06-05 | Meva Energy AB | Improved gasification system and method |
| CN112831352B (en) * | 2021-01-09 | 2021-09-07 | 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 |
| KR102312365B1 (en) * | 2021-03-26 | 2021-10-15 | 주식회사 한양 에프엔티 | High temperature reformer |
| KR102467994B1 (en) * | 2021-05-11 | 2022-11-17 | 주식회사 한양 에프엔티 | High temperatue reformer with capsule type reforming furnace |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85107163A (en) * | 1984-08-17 | 1987-04-08 | 碳气技术股份公司 | Make the method for gas from carbonaceous fuel |
| CN87103885A (en) * | 1986-05-30 | 1988-01-20 | 德克萨科开发公司 | The control method of solid carbonaceous fuel gasification |
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| JPH03239797A (en) * | 1990-02-16 | 1991-10-25 | Babcock Hitachi Kk | Prevention of slag adhesion in coal gasification furnace |
| CN1221446A (en) * | 1996-05-20 | 1999-06-30 | 株式会社日立制作所 | Coal gasification apparatus, coal gasification method and integrated coal gasification combined power generating system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5821482A (en) * | 1981-07-31 | 1983-02-08 | Electric Power Dev Co Ltd | Method and apparatus for feeding raw material slurry to coal gasification furnace |
-
2002
- 2002-02-12 JP JP2002034173A patent/JP4085239B2/en not_active Expired - Fee Related
-
2003
- 2003-02-06 WO PCT/JP2003/001282 patent/WO2003068894A1/en active Application Filing
- 2003-02-06 CN CNB038036053A patent/CN100447221C/en not_active Expired - Fee Related
- 2003-02-06 AU AU2003207084A patent/AU2003207084A1/en not_active Abandoned
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4773917A (en) * | 1983-03-28 | 1988-09-27 | Babcock-Hitachi Kabushiki Kaisha | Coal gasifier |
| CN85107163A (en) * | 1984-08-17 | 1987-04-08 | 碳气技术股份公司 | Make the method for gas from carbonaceous fuel |
| CN87103885A (en) * | 1986-05-30 | 1988-01-20 | 德克萨科开发公司 | The control method of solid carbonaceous fuel gasification |
| JPH03239797A (en) * | 1990-02-16 | 1991-10-25 | Babcock Hitachi Kk | Prevention of slag adhesion in coal gasification furnace |
| CN1221446A (en) * | 1996-05-20 | 1999-06-30 | 株式会社日立制作所 | Coal gasification apparatus, coal gasification method and integrated coal gasification combined power generating system |
Also Published As
| Publication number | Publication date |
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| CN1630701A (en) | 2005-06-22 |
| WO2003068894A1 (en) | 2003-08-21 |
| JP4085239B2 (en) | 2008-05-14 |
| JP2003231888A (en) | 2003-08-19 |
| AU2003207084A1 (en) | 2003-09-04 |
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Effective date of registration: 20160608 Address after: Tokyo, Japan, Japan Patentee after: Hitachi Ltd. Patentee after: Mitsubishi Hitachi Power System Ltd. Address before: Tokyo, Japan, Japan Patentee before: Hitachi Ltd. Patentee before: Babucock-Hitachi Kabushiki Kaisha |
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