CN1746270A - Gasification of dry-powder solid fuel - Google Patents
Gasification of dry-powder solid fuel Download PDFInfo
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- CN1746270A CN1746270A CN 200510096192 CN200510096192A CN1746270A CN 1746270 A CN1746270 A CN 1746270A CN 200510096192 CN200510096192 CN 200510096192 CN 200510096192 A CN200510096192 A CN 200510096192A CN 1746270 A CN1746270 A CN 1746270A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
A gasification of solid dry-powder fuel consists of solid dry powder preparation, dry powder fuel delivery and charge process, gasification process and coarse gas heat exchange, purification and wash processes. The method is carried out by feeding solid fuel dry powder obtained from powder maker into charger through power selector, powder collector and hopper, gasification reacting fluidized dry powder in charger with oxygen or oxygen-enriched wet mixture from gasification furnace top, chill washing the produced coarse gas, heat exchanging from radiant boiler and convection boiler on gasification furnace, lowering temperature, premixing from piping mixer and washing water, washing and purifying in gas washer, and delivering the cleaned gas for the next step. It achieves low cost, high efficiency, less consumption and simple apparatus.
Description
Technical field
The present invention relates to the preparation method that derived energy chemical and resource cleaning efficiently utilize a kind of synthetic gas in the field or fuel gas, particularly relate to a kind of gasification process of dry-powder solid fuel.
Background technology
As everyone knows, the partial oxidation process that contains hydrocarbon material produces synthetic gas or the fuel gas technology is one of important chemical monotechnics, causes that people pay much attention to, since last century early fifties until now, through the continuous progress of 50 or six ten years technical elements, obtained using widely.The development at home and abroad of fixed bed, fluidized-bed, entrained flow bed gasification technology obtains great success, especially at home Energy resources well sold and in short supply day by day today, entrained flow bed gasification technology is because of its gasification index is good, efficient energy-saving, wide adaptability, and environment friendly enjoys the favor of numerous manufacturers.
Entrained flow bed gasification technology has dry coal powder airflow bed gasification, the gasification of wet method slip etc.The Shell gasification technology is the comparatively successful dry coal powder gasification technology of a kind of industrialization, the employing multi-nozzle is reinforced, the number of nozzle is many, the conveying and metering Controlling System complexity of dried coal powder, increased the uncertain factor of the normal operation that influences vapourizing furnace, the device that is used for synthetic gas production at present is by the achievement that does not have industrialization to move now, moreover this gasification installation input expense is higher, and running cost is also high; Wet method slip gasification technology has the polynary slurry gasification technology of coal water slurry gasification and domestic-developed etc., used and promoted on the how tame at home production equipment, but in the slip of similar this wet method gasification, contain 40% the moisture of having an appointment, cause its gasification efficiency on the low side, the consumption of raw material and oxygen is higher.
Summary of the invention
The objective of the invention is in order to overcome disadvantages of background technology, and it is low to provide a kind of gasification installation to drop into expense, the gasification of dry-powder solid fuel that raw material consumption is low and gasification efficiency is high.
The object of the present invention is achieved like this: a kind of gasification of dry-powder solid fuel, comprise the preparation of solid fuel dry powder, the conveying of dry powder fuel reinforced process, gasification and raw gas heat exchange purification and washing process, it is characterized in that: described solid fuel dry powder be prepared as with granularity less than the 10mm solid fuel after metering with send into powder-making machine 1 from the hot blast of hotblast stove 7 and carry out solid-fuelled powder process and drying, the hot blast temperature that enters powder-making machine 1 is controlled at 180～300 ℃, oxygen level is controlled at less than 0.5%, and the temperature that goes out powder-making machine 1 is controlled at 80～200 ℃; Under the hot blast strength drives, solid fuel dry powder enters powder selector 2 along pipeline 17, solid fuel dry powder qualified in the powder selector 2 enters powder collector 3 at the transmitting power effect lower edge pipeline 19 that induced draft fan 26 provides, the dry powder of collecting in the powder collector 3 enters hopper 4 along pipeline 22, the medium gas of pipeline 20 is hopper 4 pressurizations simultaneously, solid fuel dry powder enters feeder 5 because of action of gravity, from pipeline 15, under 24 the fluidizing agent effect, dry powder in the feeder 5 gasification reaction district in carries out gasification reaction along pipeline 29 with sending into from vapourizing furnace 6 tops through single nozzle 34 from the oxygen of pipeline 12 or oxygen enrichment and steam mixture with fluidized, after red-hot raw gas of producing or the washing of process Quench, baffling upwards flows to vapourizing furnace 6 lateral gas exits, leave vapourizing furnace 6 and directly enter tube mixer 41 along pipeline 40, with enter gas scrubber 11 after the washing water pre-mixing from pipeline 44 and further be able to washing, purifying, clean coal gas send subsequent processing to use through pipeline 45, and gas scrubber 11 bottom wash water send vapourizing furnace 6 bottom water-baths to do make up water by pump 42 along pipeline 36.
A kind of gasification of dry-powder solid fuel, comprise the preparation of solid fuel dry powder, the conveying of dry powder fuel reinforced process, gasification and raw gas heat exchange purification and washing process, it is characterized in that: described solid fuel dry powder be prepared as with granularity less than the 10mm solid fuel after metering with send into powder-making machine 1 from the hot blast of hotblast stove 7 and carry out solid-fuelled powder process and drying, the hot blast temperature that enters powder-making machine 1 is controlled at 180～300 ℃, oxygen level is controlled at less than 0.5%, and the temperature that goes out powder-making machine 1 is controlled at 80～200 ℃; Under the hot blast strength drives, solid fuel dry powder enters powder selector 2 along pipeline 17, solid fuel dry powder qualified in the powder selector 2 enters powder collector 3 at the transmitting power effect lower edge pipeline 19 that induced draft fan 26 provides, the dry powder of collecting in the powder collector 3 enters hopper 4 along pipeline 22, the medium gas of pipeline 20 is hopper 4 pressurizations simultaneously, solid fuel dry powder enters feeder 5 because of action of gravity, from pipeline 15, under 24 the fluidizing agent effect, dry powder in the feeder 5 gasification reaction district in carries out gasification reaction along pipeline 29 with sending into from vapourizing furnace 6 tops through single nozzle 34 from the oxygen of pipeline 12 and water vapour or oxygen enrichment and steam mixture with fluidized, after the red-hot raw gas of producing washs through Quench, after the heat exchange cooling of vapourizing furnace 6 bottom radiant boilers or vapourizing furnace 6 bottom radiant boilers and the counter current boiler 9 that is connected with vapourizing furnace 6 gas exits, after tube mixer 41 and washing water pre-mixing, enter gas scrubber 11 and further be able to washing, purifying from pipeline 44, clean coal gas send subsequent processing to use through pipeline 45, and gas scrubber 11 bottom wash water send vapourizing furnace 6 bottom water-baths to do make up water by pump 42 along pipeline 36.
The present invention compared with prior art has the following advantages:
1, gasified raw material wide material sources, raw material comprises the solid matter of all carbon containing protiums such as coal, refinery coke, pitch, residue, changes into CO, H through a kind of gasification of dry-powder solid fuel
2, CO
2Unstripped gas for main ingredient;
2, because gasified raw material adopts the dry powder charging, the service temperature of vapourizing furnace is at 1200～1800 ℃, the transformation efficiency height of carbon, and consumption of raw materials is lower;
3, vapourizing furnace adopts water wall structure; built-in coil pipe of flame retardant coating or tubulation water wall in the vapourizing furnace; the work-ing life of protection and prolongation vapourizing furnace refractory materials; gasified raw material is sent into the vapourizing furnace reaction zone in the mode that single nozzle sprays down; gasification is reinforced simple, and the raw gas of generation and slag and stream are descending along the vapourizing furnace vertical direction, after Quench or heat exchange cooling; the solid slag major part immerses the furnace bottom water-bath because of downward inertia, discharges through slag ladle.This gasification process purge mode is simple, and the amount of dust that raw gas carries is low;
4, present method to greatest extent fully reasonable use the raw gas part physics heat of carrying, the damp and hot mode with byproduct steam that the red-hot raw gas that gasifier water-cooling wall, vapourizing furnace bottom radiant boiler, counter current boiler produce gasification carries reclaims timely and effectively;
5, the preparation of present method dry powder fuel and carry to adopt seal form, the gasification temperature height, the efficiency of carbon conversion height, waste water, waste residue, discharge amount of exhaust gas are little, environmentally friendly.
Description of drawings
Fig. 1 is the structural representation of equipment required for the present invention.
The tool present embodiment
As shown in Figure 1, comprise the preparation of solid fuel dry powder, the conveying of dry powder fuel reinforced process, gasification and raw gas heat exchange purification and washing process.Form the solid fuel pulverized coal preparation system by powder-making machine 1, hotblast stove 7, powder selector 2, powder collector 3, induced draft fan 26, preparation solid fuel (coal, refinery coke, pitch, coke etc.) dry powder is with carrier gas (N
2Or CO
2) be delivery medium, single-row charging system through hopper 4 and feeder 5 compositions is vapourizing furnace 6 feedings continuously, vapourizing furnace 6 is the water-cooled wall-like structure, the mode that the mixture of dry-powder solid fuel and oxygen or oxygen enrichment and water vapor sprays down with single nozzle from vapourizing furnace 6 tops through nozzle 34 is sent into and is carried out gasification reaction in the gasification reaction district (vapourizing furnace 6 burner hearths), produce raw gas, after red-hot raw gas washs through Quench, heat exchange cooling through vapourizing furnace 6 bottom radiant boilers or vapourizing furnace 6 bottom radiant boilers and the counter current boiler 9 that is connected with vapourizing furnace 6 gas exits, by-product steam, fully reasonable use the raw gas part physics heat of carrying.Most of lime-ash is discharged from vapourizing furnace 6 bottom slag ladles 8, and raw gas is with further being able to washing, purifying after enter gas scrubber 11 after tube mixer 41 and the washing water pre-mixing from pipeline 44, and comparatively clean coal gas send subsequent processing to use.
Described solid fuel dry powder is prepared as granularity less than the 10mm solid fuel, send in the lump through the solid-fuel conduit road 14 of powder-making machine 1 inlet and from the hot blast of hotblast stove 7 after metering and carry out solid-fuelled powder process and drying in the powder-making machine 1, the hot blast temperature that enters powder-making machine 1 is controlled at 180～300 ℃, oxygen level is controlled at less than 0.5%, and the temperature that goes out powder-making machine 1 is controlled at 80～200 ℃; Under the hot blast strength drives, solid fuel dry powder enters powder selector 2 along pipeline 17, the thicker particle of granularity is isolated through pipeline 16 by powder selector 2 and is returned powder-making machine 1 inlet in the powder selector 2, (moisture content is less than 10% for solid fuel dry powder qualified in the powder selector 2, optimum moisture content is less than 2%, 70% granularity is less than 200 orders, optimum size 85% is less than 200 orders), these solid fuel dry powder are under the transmitting power effect that induced draft fan 26 provides, enter powder collector 3 along pipeline 19, in powder collector 3, carry wind to separate with solid fuel dry powder, carry wind to enter induced draft fan 26 by pipeline 27, in order to keep the moisture balance carried in the wind and the maximum utilization of hot blast energy, go out the conveying wind part emptying of induced draft fan 26, a part enters the dry-heat air of the high-temperature gas mixing of hotblast stove 7 recycles and hotblast stove 7 generations as pulverized coal preparation system through pipeline 13.In another program, also can adopt temperature at 180～300 ℃, oxygen level is dry and carries wind regime less than 0.5% industrial gaseous waste.The dry powder of collecting in the powder collector 3 enters hopper 4 along pipeline 22.
Solid fuel dry powder in the described powder collector 3 is periodically to enter hopper 4, and dry powder is added to a certain degree in the hopper 4, and the valve 47 on the pipeline 22 is closed, and (medium gas is selected N for use to the medium gas of pipeline 20
2, CO
2Or refrigerative raw gas) is hopper 4 pressurizations, pressure-controlling is in 0～8.0MPa scope, when the pressure of hopper 4 and feeder 5 equate or hopper 4 slightly higher than feeder 5 pressure, valve 48 on the opening conduits 23, solid fuel dry powder enters feeder 5 because of action of gravity, when the dry powder of hopper 4 all adds feeder 5, valve-off 48, open valve 28, medium gas carries a small amount of dry powder and enters pipeline 19 through pipeline 18 in the hopper 4, and the pressure of hopper 4 is reduced to normal pressure, valve-off 28, open valve 47, hopper 4 begins to accept solid fuel dry powder.Present method is kept all the time a certain amount of solid fuel dry powder in the feeder 5, satisfy carrying out continuously of gasification.Feeder 5 bottoms are a dry powder fluidization regions, and the dry powder fluidizing agent is a medium gas, and medium gas can be selected N for use
2, CO
2Or the refrigerative raw gas, dry powder is delivered to gasification single nozzle 34 with the mode of movement of fluidized along pipeline 29.It is that vapourizing furnace 6 is reinforced that the feed way of feeder 5 also can adopt the mode of movement+fine coal transferpump array mode of fluidized, and this mode is not shown in the accompanying drawings.
The gas under pressure of hopper 4 is provided by medium gas delivery manifold 15, regulate control by valve 21, enter hopper 4 along pipeline 20, the fluidisation delivery medium gas of feeder 5 is provided by house steward 15, enter the dry powder fluidization regions of feeder 5 bottoms along pipeline 24, make solid fuel dry powder be in fluidized state, can steadily feed in raw material for vapourizing furnace 6.
Described gasification reaction material---solid fuel dry powder is sent into vapourizing furnace 6 by single nozzle 34, the mixture of oxygen or oxygen enrichment and water vapor is sent into vapourizing furnace 6 through pipeline 12 and single nozzle 34, described vapourizing furnace 6 is the water-cooled wall-like structure, the water-cooled wall-like structure is coil pipe or tubulation water wall, pipeline 32 is vapourizing furnace 6 water wall water inlet pipes, and pipeline 30 is vapourizing furnace 6 water wall steam outlet pipes; Pipeline 43 is red-hot raw gas shock chilling medium inlet pipe; Single nozzle 34 places vapourizing furnace 6 tops, send reaction mass to go into gasification reaction district (vapourizing furnace 6 burner hearths) in the mode that single nozzle sprays down, in 1200～1800 ℃ of temperature ranges, carries out gasification reaction under 0～8.0MPa pressure, generates red-hot raw gas; Raw gas is cooled to 180～300 ℃ and be in state of saturation from the shock chilling medium (shock chilling medium is selected water or cooled coal gas or steam for use) of pipeline 43 in the cinder notch bottom, the slag that gasification produces solidifies rapidly.The most of solidified lime-ash that carries in the raw gas is because the effect of mass force is downwards immersed in the vapourizing furnace 6 bottom water-baths, and the lime-ash in the water-bath by vapourizing furnace 6 bottom slag valve controls, enters in the slag ladle 8, periodically effluxes then; Raw gas baffling then upwards flows to vapourizing furnace 6 lateral gas exits, leaves vapourizing furnace 6 and directly enters tube mixer 41 along pipeline 40.Raw gas mixes in tube mixer 41 and from the water of pipeline 44, the a small amount of flying dust that carries is by water infiltration, be easy to water washing cleaning, the mixture of rough coal G﹠W enters in the water-bath of gas scrubber 11 bottoms subsequently, raw gas is by water-bath with from the further washing, purifying of washing water water of pipeline 46, clean raw gas temperature is 150～280 ℃ and sends into subsequent processing along pipeline 45 and use, gas scrubber 11 bottom wash water send vapourizing furnace 6 bottom water-baths to do make up water or miscellaneous equipment is done make up water by pump 42 along pipeline 36, and vapourizing furnace 6 bottom water bath waters efflux processing along pipeline 35.
In other method, raw gas in the cinder notch bottom by from below the steam of pipeline 43 or the water Quench to 900 ℃, the slag that gasification produces solidifies rapidly, the descending vapourizing furnace of raw gas 6 bottoms are cooled to below 600 ℃ by vapourizing furnace 6 bottom radiant boilers, and the most of solidified lime-ash that carries in the raw gas is because the effect of mass force downwards, immerse in the vapourizing furnace 6 bottom water-baths, lime-ash in the water-bath is periodically entered in the slag ladle 8 by the slag valve control of vapourizing furnace bottom, effluxes then; Raw gas baffling then upwards flows to vapourizing furnace 6 lateral gas exits, leaves vapourizing furnace 6 and enters tube mixer 41 along pipeline 40; Pipeline 33 is the radiant boiler water inlet pipe, pipeline 31 radiant boiler steam outlet pipes.Raw gas mixes in tube mixer 41 and from the water of pipeline 44, the a small amount of flying dust that carries is by water infiltration, be easy to water washing cleaning, the mixture of rough coal G﹠W enters in the water-bath of gas scrubber 11 bottoms subsequently, raw gas is by water-bath with from the further washing, purifying of the washing water of pipeline 46, clean raw gas temperature is 150～280 ℃ and sends into subsequent processing along pipeline 45 and use, gas scrubber 11 bottom wash water send vapourizing furnace 6 bottom water-baths to do make up water or miscellaneous equipment is done make up water by pump 42 along pipeline 36, and vapourizing furnace 6 bottom water bath waters efflux processing along pipeline 35.
In another method, raw gas is in the cinder notch bottom, by from below the steam of pipeline 43 or the water Quench to 900 ℃, the slag that gasification produces solidifies the descending vapourizing furnace of raw gas 6 bottoms rapidly, be cooled to below 600 ℃ by vapourizing furnace 6 bottom radiant boilers, the most of solidified lime-ash that carries in the raw gas is because the effect of mass force is downwards immersed in the vapourizing furnace 6 bottom water-baths, and the lime-ash in the water-bath is by vapourizing furnace 6 bottom slag valve controls, periodically enter in the slag ladle 8, efflux then; Raw gas baffling then upwards flows to vapourizing furnace 6 lateral gas exits, leave vapourizing furnace 6 and enter counter current boiler 9 along pipeline 37, raw gas is further lowered the temperature by heat exchange in counter current boiler 9, pipeline 38 is the water inlet pipe of counter current boiler 9, the steam outlet pipe of pipeline 39 counter current boilers 9, the raw gas temperature is reduced to below 300 ℃, a small amount of flying dust that raw gas carries is because the coal gas cooling, flow velocity reduces, be deposited on the bottom of counter current boiler 9, by the control of counter current boiler 9 bottom valves, enter in the flying dust holding tank 10, then periodically discharging; Raw gas is up to enter tube mixer 41 along pipeline 40.Raw gas is in tube mixer 41 and from the water pre-mixing of pipeline 44, the a small amount of flying dust that carries is by water infiltration, be easy to water washing cleaning, the mixture of rough coal G﹠W enters in the water-bath of gas scrubber 11 bottoms subsequently, raw gas is by water-bath with from the further washing, purifying of the washing water of pipeline 46, clean raw gas temperature is 150～280 ℃ and sends into subsequent processing along pipeline 45 and use, gas scrubber 11 bottom wash water send vapourizing furnace 6 bottom water-baths to do make up water or miscellaneous equipment is done make up water by pump 42 along pipeline 36, and vapourizing furnace 6 bottom water bath waters efflux processing along pipeline 35.
With the Shaanxi shenfu coal is that raw material is implemented operation result of the present invention.
Raw material ultimate analysis (quality) is as follows:
C 70.80
H 4.85
S 0.40
O 12.09
Aad 5.36
Mad 5.60
Thermal value: 29000j/g.
The operational condition that adopts is as follows: dried coal powder flow 2t/h; Oxygen purity 98%, oxygen flow 1180Nm
3, the steam 70kg/h of 4.5MPa, vapourizing furnace working pressure 3.0MPa, 1450 ℃ of temperature; Dry gas flow 4130Nm
3/ h, CO+H
2Content 90.50mol%, the steam 1.2t/h of by-product 4.0MPa, lime-ash total amount 136kg/h (butt).
Claims (3)
1, a kind of gasification of dry-powder solid fuel, comprise the preparation of solid fuel dry powder, the conveying of dry powder fuel reinforced process, gasification and raw gas heat exchange purification and washing process, it is characterized in that: described solid fuel dry powder be prepared as with granularity less than the 10mm solid fuel after metering with send into powder-making machine (1) from the hot blast of hotblast stove (7) and carry out solid-fuelled powder process and drying, the hot blast temperature that enters powder-making machine (1) is controlled at 180～300 ℃, and the temperature that goes out powder-making machine (1) is controlled at 80～200 ℃; Under the hot blast strength drives, solid fuel dry powder enters powder selector (2) along pipeline (17), solid fuel dry powder qualified in the powder selector (2) enters powder collector (3) at the transmitting power effect lower edge pipeline (19) that induced draft fan (26) provides, the dry powder of collecting in the powder collector (3) enters hopper (4) along pipeline (22), the next medium gas of pipeline (20) is hopper (4) pressurization simultaneously, solid fuel dry powder enters feeder (5) because of action of gravity, from pipeline (15,24) under the fluidizing agent effect, dry powder in the feeder (5) gasification reaction district in carries out gasification reaction along pipeline (29) with sending into from vapourizing furnace (6) top through single nozzle (34) from the oxygen of pipeline (12) or oxygen enrichment and steam mixture with fluidized, after red-hot raw gas of producing or the washing of process Quench, baffling upwards flows to the lateral gas exit of vapourizing furnace (6), leave vapourizing furnace (6) and directly enter tube mixer (41) along pipeline (40), with enter gas scrubber (11) after the washing water pre-mixing from pipeline (44) and further be able to washing, purifying, clean coal gas send subsequent processing to use through pipeline (45), and gas scrubber (11) bottom wash water send vapourizing furnace (6) bottom water-bath to do make up water by pump (42) along pipeline (36).
2, a kind of gasification of dry-powder solid fuel, comprise the preparation of solid fuel dry powder, the conveying of dry powder fuel reinforced process, gasification and raw gas heat exchange purification and washing process, it is characterized in that: described solid fuel dry powder be prepared as with granularity less than the 10mm solid fuel after metering with send into powder-making machine (1) from the hot blast of hotblast stove (7) and carry out solid-fuelled powder process and drying, the hot blast temperature that enters powder-making machine (1) is controlled at 180～300 ℃, and the temperature that goes out powder-making machine (1) is controlled at 80～200 ℃; Under the hot blast strength drives, solid fuel dry powder enters powder selector (2) along pipeline (17), solid fuel dry powder qualified in the powder selector (2) enters powder collector (3) at the transmitting power effect lower edge pipeline (19) that induced draft fan (26) provides, the dry powder of collecting in the powder collector (3) enters hopper (4) along pipeline (22), the next medium gas of pipeline (20) is hopper (4) pressurization simultaneously, solid fuel dry powder enters feeder (5) because of action of gravity, from pipeline (15,24) under the fluidizing agent effect, dry powder in the feeder (5) gasification reaction district in carries out gasification reaction along pipeline (29) with sending into from vapourizing furnace (6) top through single nozzle (34) from the oxygen of pipeline (12) or oxygen enrichment and steam mixture with fluidized, after red-hot raw gas of producing or the washing of process Quench, after the heat exchange cooling of vapourizing furnace (6) bottom radiant boiler or vapourizing furnace (6) bottom radiant boiler and the counter current boiler (9) that is connected with vapourizing furnace (6) gas exit, after tube mixer (41) and washing water pre-mixing, enter gas scrubber (11) and further be able to washing, purifying from pipeline (44), clean coal gas send subsequent processing to use through pipeline (45), and gas scrubber (11) bottom wash water send vapourizing furnace (6) bottom water-bath to do make up water by pump (42) along pipeline (36).
3, a kind of gasification of dry-powder solid fuel according to claim 1 and 2, it is characterized in that: described vapourizing furnace (6) is the water-cooled wall-like structure, the water-cooled wall-like structure is coil pipe or tubulation water wall, pipeline (32) is vapourizing furnace (a 6) water wall water inlet pipe, and pipeline (30) is vapourizing furnace (a 6) water wall steam outlet pipe; Pipeline (43) is red-hot raw gas shock chilling medium inlet pipe; Pipeline (33) is the radiant boiler water inlet pipe, and pipeline (31) is a radiant boiler steam outlet pipe, and single nozzle (34) places vapourizing furnace (6) top.
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| CNB2005100961921A CN1328356C (en) | 2005-10-18 | 2005-10-18 | Gasification of dry-powder solid fuel |
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| CN101747941A (en) * | 2008-12-17 | 2010-06-23 | 财团法人工业技术研究院 | The dry type of equipment for gasification and the feed system of wet double-purpose |
| CN101161792B (en) * | 2007-09-29 | 2010-11-17 | 上海惠生化工工程有限公司 | Heat recovering technique for synthetic gas production process by coal gasification |
| WO2012003766A1 (en) * | 2010-07-07 | 2012-01-12 | Kong Lingzeng | Process and reaction apparatus for preparing nitrogen-free coal fuel gas using coal and oxygen |
| CN102352268A (en) * | 2011-09-08 | 2012-02-15 | 西北化工研究院 | Method for producing synthesis gas by using coal powder as raw material |
| CN102433164A (en) * | 2011-10-20 | 2012-05-02 | 清华大学 | Entrained-flow bed gasification system and method for vapour conveyed pulverized coal |
| CN102443439A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Method for preparing synthesis gas by fixed bed pressurization and gasification |
| CN102443440A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Device for producing synthesis gas by fixed bed pressurization and gasification |
| WO2012162971A1 (en) * | 2011-05-27 | 2012-12-06 | 北京神雾环境能源科技集团股份有限公司 | Cyclone bed pulverized coal gasification method and system thereof |
| CN103146433A (en) * | 2013-03-05 | 2013-06-12 | 上海锅炉厂有限公司 | Gasifier of entrained-flow bed with single nozzle |
| CN101781586B (en) * | 2010-01-29 | 2013-06-26 | 上海锅炉厂有限公司 | High-temperature synthesis gas sensible heat recovery device |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4857407A (en) * | 1987-06-16 | 1989-08-15 | Ppg Industries, Inc. | Low modulus interlayer |
| CN1219857C (en) * | 2002-09-27 | 2005-09-21 | 中国科学院山西煤炭化学研究所 | Solid slag-discharing dry-powder air-current bed gasification process and apparatus |
-
2005
- 2005-10-18 CN CNB2005100961921A patent/CN1328356C/en active Active
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| CN101161792B (en) * | 2007-09-29 | 2010-11-17 | 上海惠生化工工程有限公司 | Heat recovering technique for synthetic gas production process by coal gasification |
| CN101747941A (en) * | 2008-12-17 | 2010-06-23 | 财团法人工业技术研究院 | The dry type of equipment for gasification and the feed system of wet double-purpose |
| CN101747941B (en) * | 2008-12-17 | 2013-10-16 | 财团法人工业技术研究院 | Dry and wet double-purpose feeding system for gasifying equipment |
| CN101781586B (en) * | 2010-01-29 | 2013-06-26 | 上海锅炉厂有限公司 | High-temperature synthesis gas sensible heat recovery device |
| WO2012003766A1 (en) * | 2010-07-07 | 2012-01-12 | Kong Lingzeng | Process and reaction apparatus for preparing nitrogen-free coal fuel gas using coal and oxygen |
| CN102443440A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Device for producing synthesis gas by fixed bed pressurization and gasification |
| CN102443439A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Method for preparing synthesis gas by fixed bed pressurization and gasification |
| WO2012162971A1 (en) * | 2011-05-27 | 2012-12-06 | 北京神雾环境能源科技集团股份有限公司 | Cyclone bed pulverized coal gasification method and system thereof |
| CN102352268B (en) * | 2011-09-08 | 2013-07-31 | 西北化工研究院 | Method for producing synthesis gas by using coal powder as raw material |
| CN102352268A (en) * | 2011-09-08 | 2012-02-15 | 西北化工研究院 | Method for producing synthesis gas by using coal powder as raw material |
| CN102433164A (en) * | 2011-10-20 | 2012-05-02 | 清华大学 | Entrained-flow bed gasification system and method for vapour conveyed pulverized coal |
| CN103146433A (en) * | 2013-03-05 | 2013-06-12 | 上海锅炉厂有限公司 | Gasifier of entrained-flow bed with single nozzle |
| CN103146433B (en) * | 2013-03-05 | 2014-09-03 | 上海锅炉厂有限公司 | Gasifier of entrained-flow bed with single nozzle |
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