CN101024782B - Dense-phase conveying-bed coal pressurizing gasifying apparatus and method - Google Patents
Dense-phase conveying-bed coal pressurizing gasifying apparatus and method Download PDFInfo
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- CN101024782B CN101024782B CN200710020990A CN200710020990A CN101024782B CN 101024782 B CN101024782 B CN 101024782B CN 200710020990 A CN200710020990 A CN 200710020990A CN 200710020990 A CN200710020990 A CN 200710020990A CN 101024782 B CN101024782 B CN 101024782B
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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
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
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- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Abstract
The invention relates to a dense phase conveying bed coal preesurized gasification device and a gasification method. The gasification reactor includes pressure case, mixing section, lifting section, and conveying section. The mixing section adopts low flow speed, and has inlet for coal limestone, assistant gasification agent, and has grid plate, scum pipe, air chamber and main gasification agent inlet. The lifting section has assistant air or oxygen inlet and adopts high flow velocity mode. The convey section adopts middle velocity mode, and the outlet of convey section has two high efficiency cyclone separator. The material return mouth of material return section is inserting into gasification reactor.
Description
Technical field
The present invention relates to a kind of dense-phase conveying-bed coal pressurizing gasifying apparatus and method, belong to the Coal Gasification Technology field.
Background technology
Gasification is the basis of many clean coal technologies of new generation, as burying CO with the leading Poly-generation energy resource system of gasification, integrated gasification combined cycle plants (IGCC) with hydrogen manufacturing and collection that coal gas turns to the basis
2Technology etc. is coupled.Gasification not only can solve the pollution problem in the direct combustion processes to a great extent, and can form the product of high value, plays important status in China's energy strategy.
At present, industrialized gasification installation mainly contains fixed bed, fluidized-bed and airflow bed gasification furnace, and all there is certain problem in these gasifying process.Fixed-bed gasification furnace be applicable to the gasification of weak cohesiveness lump coal or moulded coal, and for preventing slagging scorification, service temperature is lower to the bad adaptability of coal, and the water vapor consumption is big, and the by product tar of generation and phenol are difficult to handle; Single stove throughput is lower, and maximization has difficulties; But the fluidized-bed gasification furnace coal adaptability is wide, cost is low, the feature of environmental protection is good, water treatment system is simple, the few desulfuration in furnace of steam consumption, but efficiency of carbon conversion is lower, complex structure, and operation is also complicated; Airflow bed gasification furnace need be used pure oxygen, and investment is high, and is also relatively poor to the adaptability of ash-rich and high ash melting point coal seed.At the problem that present various vapourizing furnaces exist, need development coal gasifying process of new generation, strengthen the adaptability of coal, raise the efficiency, reduce cost, make rational use of resources.
In recent years, for adapting to the demand for development of integrated gasification combined cycle plants (IGCC), the U.S. has proposed dense phase transporting bed gasification technology, this technology combines the advantage of air flow bed and fluidized-bed, good as adaptability to coal, efficiency of carbon conversion is high, investment is little, load range is wide and the response is fast, is expected to break through the bottleneck of IGCC development.The U.S. has carried out the small-scale test research of coal treatment capacity 100kg/h, result of study has shown the tempting development prospect of dense phase transporting bed gasification technology, but have following several distinct issues: (1) reactor flow velocity is too fast and the temperature of reaction efficiency of carbon conversion that causes on the low side is on the low side, and flow velocity 7～15m/s, about 900 ℃ of temperature of reaction, efficiency of carbon conversion are less than 80%; (2) heat lost by radiation of system is big, reaches 15%; (3) calorific value of coal gas is on the low side, less than 3000KJ/Nm
3At present, the how tame scientific research institution of the U.S. and other country just conducts a research, and seeks new improvement thinking, the development dense-phase conveying-bed coal pressurizing gasifying apparatus.
In China, existing industrialization Coal Gasification Technology and equipment (fixed bed, fluidized-bed and gas-flow bed gasifying apparatus) are long-term by abroad being monopolized.The coal resources that dense phase transporting bed gasification technology is particularly suitable for handling the abundant high-sulfur of China's reserves, high ash, high ash melting point have carried out the R﹠D work of this gasification installation abroad prior to China; The current domestic independent research and development capacity that possessed, close the gap is developed the dense-phase conveying-bed coal pressurizing gasifying apparatus that is suitable for China's national situation, has independent intellectual property right in the short period of time, avoids repeating away the road for development that introduction absorbs.
Summary of the invention
Technical problem: at the problem of present various industrial gasification stoves and the existence of dense-phase conveying-bed coal pressurizing gasifying novel process, the present invention proposes a kind of dense-phase conveying-bed coal pressurizing gasifying apparatus and method, it is a kind of wide to coal adaptability that purpose is to provide, particularly be suitable for handling the abundant high-sulfur of China's reserves, high ash, high-ash-fusion coal, and gasification efficiency of carbon conversion height, caloric power of gas height, investment is low, environmental-protecting performance is superior gasification process and device.
Technical scheme: in the dense-phase conveying-bed coal pressurizing gasifying apparatus of the present invention, gasifying reactor is arranged in the pressure vessel, is divided into mixing section from bottom to top in gasifying reactor, promotes the section and the section of transporting; Wherein, the side of mixing section is provided with coal and Wingdale import, auxiliary gasifying agent import, one-level returning charge mouth and secondary returning charge mouth from bottom to top, and the bottom is provided with air distribution plate, scum pipe, air compartment and main vaporized chemical import; Promote section and formed by mixing section and the section of transporting contraction, and be provided with auxiliary air or oxygen inlet, height is greater than mixing section, and diameter is 0.4～0.7 times of mixing section; The section of transporting height is greater than promoting section, and diameter is identical with mixing section, outlet polyphone one-level efficient cyclone separator; The top outlet of one-level efficient cyclone separator connects the secondary efficient cyclone separator, the bottom that secondary efficient cyclone separator bottom all is connected to secondary material blanking tube, secondary material blanking tube connects secondary J type returning charge valve, and the other end of secondary J type returning charge valve becomes 30～miter angle with the gasifying reactor axis and links to each other with secondary returning charge mouth; The bottom of one-level efficient cyclone separator is connected to the one-level material blanking tube, and the bottom of one-level material blanking tube is connected to one-level J type returning charge valve, and the other end of one-level J type returning charge valve becomes 30～miter angle with the gasifying reactor axis and links to each other with one-level returning charge mouth.
The gasification process of dense-phase conveying-bed coal pressurizing gasifying apparatus of the present invention is to adopt high-temperature operation temperature in the identical high working pressure of 2.0～3.0MPa, 1000～1100 ℃, 50～100 high circulation ratio and solid flux greater than 200kg/m
2S dense-phase conveying fluidised form and different operating speeds, concrete mode is: with inert bed material, coal and Wingdale, join mixing section, vaporized chemical is mixed by the air or oxygen of the required whole superheated vapours of gasification and required 90%, the mode that adopts classification to add, 60% adds from air compartment, and 40% adds from mixing section; Mixing section adopts the low flow velocity operation of 2.5～4.5m/s, inert bed material, coal and Wingdale and vaporized chemical thorough mixing, the coal fugitive constituent deviate from vaporized chemical in air or oxygen generation combustion reactions the gasification reaction heat is provided, steam in the vaporized chemical and coal generation part gasification reaction produce coal gas and semicoke then; Extra 10% required air or oxygen of the gasification a spot of generation coal gas that burns that adds in promoting section, for gasification reaction and equipment cooling provide thermal source, keep whole reactor to bring up to 7.5～12.5m/s along Cheng Wendu uniformity and gas speed that will the section of lifting, in the turbulent mode gas-solid mixture of mixing section is risen to the section of transporting and continue reaction, the middle flow velocity operation scheme of the section of transporting employing 5～7m/s; The raw gas that generates purifies by the one-level efficient cyclone separator and the secondary efficient cyclone separator of polyphone, the solid particulate that separates falls into material blanking tube and the J type returning charge valve from the device bottom, in the returning charge valve, add simultaneously some median sizes and be the thin bed material of inertia about 0.2mm, make do not react completely semicoke and Wingdale successfully enter gasifying reactor and carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by 50～100 high circulation ratio from the returning charge mouth of mixing section.Adopt the two-stage efficient cyclone separator to separate solid particulate in the coal gas of generation (being mainly CaS that coke, the desulfurization completely of flying dust, unreacted produce and thin bed material etc.), total efficiency of separation is greater than 99.5%; The material returning device of two-stage efficient cyclone separator bottom is a J type returning charge valve, takes independent returning charge mode, and two-stage is not disturbed mutually; In the returning charge valve, add the thin bed material of a certain amount of inertia and guarantee high circulation ratio, make do not react completely semicoke and Wingdale carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation.
Described low flow velocity is 2.5～4.5m/s, and middle flow velocity is 5～7m/s, and high flow rate is 7.5～12.5m/s, high working pressure is 2.0～3.0MPa, middle high-temperature operation temperature is 1000～1100 ℃, and high circulation ratio is 50～100, and dense-phase conveying refers to that the solid flux is greater than 200kg/m
2S.
Beneficial effect: apparatus and method of the present invention combine the advantage of fluidized-bed and entrained flow gasification technology, and have following characteristic and advantage at the problem of present various industrial gasification stoves and the existence of dense-phase conveying-bed coal pressurizing gasifying novel process:
1, reactor adopts mixing section, promotes section and three sections designs of the section of transporting, and operation scheme adopts different operating speeds, identical high working pressure, middle high-temperature operation temperature and dense-phase conveying fluidised form.
2, mixing section adopts low flow velocity operation scheme, and air distribution plate is set and adds inert bed material and form stable emulsion zone and thermal source, can prolong the residence time of coal grain, realizes the well blend of gas-solid.
3, vaporized chemical adopts classification to add mode, vaporized chemical is mixed by superheated vapour and air or oxygen, and 40% vaporized chemical adds from mixing section, and 60% vaporized chemical adds from air compartment, help the reasonable distribution of mixing section regional temperature, prevent the too high and coking of local temperature.Promote extra 10% required air or oxygen of the gasification a spot of generation coal gas that burns that adds of section, for gasification reaction and equipment cooling provide thermal source, make the gasifier upper temp not reason continue gasification reaction and equipment cooling and reduce; It is less to promote the section cross section, and the turbulence of gas-solid is further strengthened in the adding of air or oxygen, has strengthened the interaction between air-flow and the particle; The transformation efficiency of carbon and the removal efficiency of sulfurous pollutants are improved.
4, adopt the two-stage efficient cyclone separator,, improve the quality of coal gas, be particularly suitable for the gasification of dirty coal kind with the solid impurity in the high efficiency separation coal gas.
5, consider the pressure reduction of first and second grade cyclonic separator, adopted two-stage independence returning charge mode, be convenient to control; In addition, in the returning charge valve, add the thin bed of a certain amount of inertia and expect to guarantee the high circulation ratio of semicoke and Wingdale, help recycle stock the flowing and returning charge smooth and easy of cyclonic separator bottom material blanking tube, carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants simultaneously.
6, adopt pressurized gasification, the volume of device is little, the coal treatment capacity is big, gasification efficiency is high.
7, the adaptability to coal is good, the abundant high-sulfur of China's reserves that is particularly suitable for gasifying, high ash, high-ash-fusion coal.
Description of drawings
Fig. 1 is a dense-phase conveying-bed coal pressurizing gasifying apparatus structural representation of the present invention.
Fig. 2 is a dense-phase conveying-bed coal pressurizing gasifying apparatus implementation system synoptic diagram of the present invention.
Have among the above figure: gasifying reactor 1, pressure vessel 2, one-level efficient cyclone separator 3, one-level material blanking tube 4, one-level J type returning charge valve 5, secondary efficient cyclone separator 6, secondary material blanking tube 7, secondary J type returning charge valve 8, mixing section 9, promote section 10, the section of transporting 11, coal and Wingdale import 12, auxiliary gasifying agent import 13, one-level returning charge mouth 14, secondary returning charge mouth 15, air distribution plate 16, scum pipe 17, air compartment 18, auxiliary air or oxygen inlet 19, main vaporized chemical import 20, waste heat boiler 21, dust separation device 22, association circulating power generation system 23, CFB boiler 24, well heater 25, mixing tank 26.Coal and Wingdale A, main vaporized chemical B, auxiliary gasifying agent C, air or oxygen D, gas-solid mixture E, raw gas F, flash trapping stage material G, one-level returning charge H, first class purification coal gas I, secondary separating material J, secondary returning charge K, high temperature purified gas L, slag M, Low Temperature Steam N, low temperature purified gas O, cleaned coal gas P, ash discharge Q, high-temperature steam R, superheated vapour S, vaporized chemical T, electric energy U.
Embodiment
Be divided into mixing section 9, promote 11 3 sections of section 10 and the sections of transporting referring to accompanying drawing 1 gasifying reactor 1, adopt the identical high working pressure of 2.0～3.0MPa, 1000～1100 ℃ middle high-temperature operation temperature and solid flux greater than 200kg/m
2The dense-phase conveying fluidised form of s, but operating speed difference.Mixing section 9 adopts the low flow velocity operation scheme of 2.5～4.5m/s, and its function is to realize the well blend of coal and Wingdale A, vaporized chemical T and I and II returning charge, and devolatilization, burning and the partial gasification reaction of carrying out coal; For realizing this function, in mixing section 9, add the inert bed material of a certain amount of suitable granularity, as quartz sand, guarantee at mixing section 9 bottoms formation emulsion zone; For improving reactivity worth, adopt median size than the duff particle; Vaporized chemical T is mixed by superheated vapour and air or oxygen, the mode that adopts classification to add, and 40% vaporized chemical T adds from mixing section 9, and 60% vaporized chemical T adds from the main vaporized chemical import 20 of air compartment 18; The bed material adds the hot coal grain rapidly, and the coal fugitive constituent is deviate from air or oxygen generation combustion reactions provides the gasification reaction heat, and steam and coal generation part gasification reaction produce coal gas and semicoke then.Promoting section 10 and the section of transporting 11 is main sections of gasification reaction and desulphurization reaction, and the semicoke that generates behind mixing section 9 partial gasifications is at this section gasification, the H that Wingdale produces gasification
2S removes.For making these two sections can not continue generating gasification thermo-negative reaction and the reduction of equipment cooling temperature, promoting extra 10% required air or oxygen of the gasification a spot of generation coal gas that burns that adds of section 10, for gasification reaction and equipment cooling provide thermal source, keep whole reactor along the Cheng Wendu uniformity, improve the gasification working conditions of middle and upper part; In addition, it is less to promote section 10 cross sections, and the turbulence of gas-solid is further strengthened in the adding of 10% air or oxygen, has strengthened the interaction between air-flow and the particle, can improve gasification reaction and sulfurous pollutants removes speed.Promote the high flow rate operation scheme that section 10 adopts 7.5～12.5m/s, the gas-solid mixture of mixing section 9 is risen to the section of transporting 11 in the turbulent mode, the section of transporting 11 adopts the middle flow velocity operation scheme of 5～7m/s, to prolong the particulate residence time, carry the removal efficiency of high-carbon transformation efficiency and pollutent.Adopt the two-stage efficient cyclone separator to separate solid particulate in the coal gas of generation (being mainly CaS that coke, the desulfurization completely of flying dust, unreacted produce and thin bed material etc.), total efficiency of separation is greater than 99.5%; The material returning device that the two-stage efficient cyclone separator separates the bottom is a J type returning charge valve, takes independent returning charge mode, and two-stage is not disturbed mutually; In the returning charge valve, add the thin bed material of a certain amount of inertia and guarantee 50～100 high circulation ratio, make do not react completely semicoke and Wingdale carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation.
Concrete structure is: whole device is arranged in the pressure vessel 2, and gasifying reactor 1 is divided into mixing section 9 from bottom to top, promotes section 10 and the section of transporting 11.The side of mixing section 9 is provided with coal and Wingdale import 12, auxiliary gasifying agent import 13, one-level returning charge mouth 14 and secondary returning charge mouth 15 from bottom to top, the bottom is provided with air distribution plate 16 and scum pipe 17, air distribution plate 16 bottoms are air compartment 18, the side of air compartment 18 is provided with main vaporized chemical import 20, and scum pipe 17 passes air compartment 18 and pressure vessel 2 leads to outside the device; Promote section 10 and formed by mixing section 9 and the section of transporting 11 contractions, be provided with auxiliary air or oxygen inlet 19, height is greater than mixing section 9, and diameter is 0.4～0.7 times of mixing section 9; The section of transporting 11 height are greater than promoting section 10, and diameter is identical with mixing section 9; The outlet of the section of transporting 11 connects one-level efficient cyclone separator 3, one-level efficient cyclone separator 3 bottoms are connected to one-level material blanking tube 4, the bottom of one-level material blanking tube 4 is connected to one-level J type returning charge valve 5, and the other end of one-level J type returning charge valve 5 becomes 30～45 degree to be connected one-level returning charge mouth 14 with reactor axis; The outlet on one-level efficient cyclone separator 3 tops is connected to secondary efficient cyclone separator 6, spend and be arranged in the higher position for 3 one-tenth 30～45 with the one-level efficient cyclone separator, the bottom of secondary efficient cyclone separator 6 is connected to secondary material blanking tube 7, the bottom of secondary material blanking tube 7 is connected to secondary J type returning charge valve 8, and the other end of secondary J type returning charge valve 8 becomes 45～60 degree to be connected secondary returning charge mouth 15 with reactor axis; The I and II efficient cyclone separator is identical with the scantlings of the structure of J type returning charge valve, but the diameter of secondary material blanking tube 7 and secondary returning charge mouth 15 is littler than one-level.
The gasifying process flow process of implementing according to the present invention is as shown in Figure 2: earlier by coal and Wingdale import 12, a certain amount of granularity of adding is the inert bed material about 1mm mixing section 9 in, as quartz sand, guarantees can form emulsion zone in mixing section 9 bottoms; Adopt the ignition under bed Starting mode, diesel oil or Sweet natural gas and air produce 1000 ℃ of left and right sides high-temperature fuel gas after starting combustion chambers burn, by main vaporized chemical import 20, high-temperature fuel gas is sent into air compartment 18, high-temperature fuel gas enters mixing section 9 heated inert bed material after passing the aperture of air distribution plate 16.When inert bed material is heated to 500 ℃ of left and right sides by high-temperature fuel gas, coal and Wingdale A are added to mixing section 9 from coal and Wingdale import 12, reflect performance for improving reaction, coal and Wingdale all adopt the following particle of particle diameter 1mm.Inert bed material adds the hot coal grain rapidly, the coal fugitive constituent is deviate from air or oxygen generation combustion reactions provides the gasification reaction heat, bed temperature constantly raises, when bed temperature reaches 800 ℃ of left and right sides, stop to add high-temperature fuel gas, drop into vaporized chemical T, vaporized chemical T and coal generation part gasification reaction produce coal gas and semicoke.Vaporized chemical T is mixed by superheated vapour S and air or oxygen D, the mode that adopts classification to add, and 40% vaporized chemical T adds from mixing section 9, and 60% vaporized chemical T adds from the main vaporized chemical import 20 of air compartment 18.Mixing section 9 adopts the low flow velocity operation scheme of 2.5～4.5m/s, and its function is to realize the well blend of coal and Wingdale, vaporized chemical T and I and II returning charge, and devolatilization, burning and the partial gasification reaction of carrying out coal.Contain complicated ingredient gas-solid mixtures such as coal gas, semicoke, bed material, Wingdale and after promoting section 10, enter the section of transporting 11.Promoting section 10 and the section of transporting 11 is main sections of gasification reaction and desulphurization reaction, and the semicoke that generates behind mixing section 9 partial gasifications is at this section gasification, the H that Wingdale produces gasification
2S removes.For these two sections can not reduced because of continuing generating gasification thermo-negative reaction and equipment cooling temperature, add 10% required air or oxygen of gasification a spot of generation coal gas that burns promoting section 10, for gasification reaction and equipment cooling provide thermal source, keep whole reactor along the Cheng Wendu uniformity, improve the gasification working conditions of middle and upper part; In addition, because it is less to promote section 10 cross sections, the turbulence of gas-solid is further strengthened in the adding of 10% air or oxygen, has strengthened the interaction between air-flow and the particle, can improve gasification reaction and sulfurous pollutants removes speed.Promote the high flow rate operation scheme that section 10 adopts 7.5～12.5m/s, the gas-solid mixture of mixing section 9 is risen to the section of transporting 11 in the turbulent mode, the section of transporting 11 adopts the middle flow velocity operation scheme of 5～7m/s, to prolong the particulate residence time, carry the removal efficiency of high-carbon transformation efficiency and pollutent.The raw gas F that gasification generates enters the two-stage efficient cyclone separator, and to remove solid particulate in the coal gas (being mainly CaS that coke, the desulfurization completely of flying dust, unreacted produce and the thin bed material of inertia etc.), total efficiency of separation is greater than 99.5%; The material returning device of two-stage efficient cyclone separator bottom is a J type returning charge valve, takes independent returning charge mode, and two-stage is not disturbed mutually; The thin bed material of inertia that adds a certain amount of median size be in the returning charge valve about 0.2mm guarantees 50～100 high circulation ratio, makes do not react completely semicoke and Wingdale carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation.Raw gas F becomes the high temperature purified gas L that has certain dust after the two-stage efficient cyclone separator purifies, high temperature purified gas L enters waste heat boiler 21 coolings, the sensible heat of high temperature purified gas L produces Low Temperature Steam N and low temperature purified gas O after heat exchange, low temperature purified gas O becomes cleaned coal gas P behind dust separation device 22, produce electric energy U for the fuel gas generation in the association circulating power generation system 23; The ash discharge Q of dust separation device 22 and the deslagging M of gasifier 1 send into burning in the CFB boiler 24, produce high-temperature steam R, the Low Temperature Steam N that high-temperature steam R that CFB boiler 24 produces and waste heat boiler 21 produce also together again through after well heater 25 heating, becomes superheated vapour S; A superheated vapour S part produces electric energy U for the steam-electric power in the association circulating power generation system 23, and another part mixes the back with air or oxygen at mixing tank 26 and forms vaporized chemical T.
Claims (2)
1. dense-phase conveying-bed coal pressurizing gasifying apparatus, it is characterized in that: gasifying reactor (1) is arranged in the pressure vessel (2), is divided into mixing section (9) from bottom to top in gasifying reactor (1), promotes section (10) and the section of transporting (11); Wherein, the side of mixing section (9) is provided with coal and Wingdale import (12), auxiliary gasifying agent import (13), one-level returning charge mouth (14) and secondary returning charge mouth (15) from bottom to top, and the bottom is provided with air distribution plate (16), scum pipe (17), air compartment (18) and main vaporized chemical import (20); Promote section (10) and formed by mixing section (9) and the section of transporting (11) contraction, and be provided with auxiliary air or oxygen inlet (19), height is greater than mixing section (9), and diameter is 0.4～0.7 times of mixing section (9); The section of transporting (11) height is greater than promoting section (10), and diameter is identical with mixing section (9), outlet polyphone one-level efficient cyclone separator (3); The top outlet of one-level efficient cyclone separator (3) connects secondary efficient cyclone separator (6), the bottom that secondary efficient cyclone separator (6) bottom is connected to secondary material blanking tube (7), secondary material blanking tube (7) connects secondary J type returning charge valve (8), and the other end of secondary J type returning charge valve (8) becomes 30～miter angle with gasifying reactor (1) axis and links to each other with secondary returning charge mouth (15); The bottom of one-level efficient cyclone separator (3) is connected to one-level material blanking tube (4), the bottom of one-level material blanking tube (4) is connected to one-level J type returning charge valve (5), and the other end of one-level J type returning charge valve (5) becomes 30～miter angle with gasifying reactor (1) axis and links to each other with one-level returning charge mouth (14).
2. the gasification process of a dense-phase conveying-bed coal pressurizing gasifying apparatus as claimed in claim 1 is characterized in that: adopt high-temperature operation temperature in the identical high working pressure of 2.0～3.0MPa, 1000～1100 ℃, 50～100 high circulation ratio and solid flux greater than 200kg/m
2S dense-phase conveying fluidised form and different operating speeds, concrete mode is: inert bed material, coal and Wingdale are joined mixing section (9), vaporized chemical (T) is mixed by the air or oxygen (D) of the required whole superheated vapours (S) of gasification and required 90%, the mode that adopts classification to add, 60% adds from air compartment (18), and 40% adds from mixing section (9); Mixing section (9) adopts the low flow velocity operation of 2.5～4.5m/s, inert bed material, coal and Wingdale and vaporized chemical thorough mixing, the fugitive constituent of coal deviates from and vaporized chemical (T) in air or oxygen (D) combustion reactions takes place that the gasification reaction heat is provided, steam in the vaporized chemical (T) and coal generation part gasification reaction produce coal gas and semicoke then; Extra 10% required air or oxygen (D) of the gasification a spot of generation coal gas that burns that adds in promoting section (10), for gasification reaction and equipment cooling provide thermal source, keep whole reactor to bring up to 7.5～12.5m/s along Cheng Wendu uniformity and gas speed that will the section of lifting (10), in the turbulent mode gas-solid mixture (E) of mixing section (9) is risen to the section of transporting (11) and continue reaction, the middle flow velocity operation scheme of the section of transporting (11) employing 5～7m/s; The raw gas (F) that generates purifies by the one-level efficient cyclone separator (3) and the secondary efficient cyclone separator (6) of polyphone, the solid particulate that separates falls into the material blanking tube and the J type returning charge valve of separator bottom, adding simultaneously some median sizes in the returning charge valve is the thin bed material of inertia of 0.2mm, makes do not react completely semicoke and Wingdale successfully enter gasifying reactor (1) and carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by 50～100 high circulation ratio from the returning charge mouth of mixing section (9).
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| CN110819392B (en) * | 2019-11-21 | 2021-08-31 | 中国科学院工程热物理研究所 | Gasification furnace and partial gasification method |
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| CN201024157Y (en) * | 2007-04-06 | 2008-02-20 | 东南大学 | Dense phase delivery bed coal pressurized gasification device |
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2007
- 2007-04-06 CN CN200710020990A patent/CN101024782B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1721511A (en) * | 2005-07-01 | 2006-01-18 | 煤炭科学研究总院北京煤化工研究分院 | Process for pressurized gasification of dry coal fines |
| CN2846418Y (en) * | 2005-10-09 | 2006-12-13 | 西北化工研究院 | Dry powder solid fuel gasifying device |
| CN201024157Y (en) * | 2007-04-06 | 2008-02-20 | 东南大学 | Dense phase delivery bed coal pressurized gasification device |
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| Title |
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| JP昭57-190090A 1982.11.22 |
| 沈湘林,熊源泉.煤粉加压密相输送实验研究.中国电机工程学报25 24.2005,25(24),103-107. |
| 沈湘林,熊源泉.煤粉加压密相输送实验研究.中国电机工程学报25 24.2005,25(24),103-107. * |
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