CN1038846C - Gasification process and device of ash fusing fluidized bed - Google Patents
Gasification process and device of ash fusing fluidized bed Download PDFInfo
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- CN1038846C CN1038846C CN94106781A CN94106781A CN1038846C CN 1038846 C CN1038846 C CN 1038846C CN 94106781 A CN94106781 A CN 94106781A CN 94106781 A CN94106781 A CN 94106781A CN 1038846 C CN1038846 C CN 1038846C
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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
The present invention relates to a gasification process and a gasification device of an ash fusing fluidized bed. The process comprises the steps of preparing coal, supplying gases, gasifying, removing dust and recovering waste heat, wherein in the coal preparing process, the viscosity of the coal does not need breaking. The gasification device is composed of a fluidized bed gasification unit, a fused ash separation unit, a flyash circulation unit and a waste heat recovery unit, wherein a Venturi throat tube with complicated structure and difficult production is omitted in the fused ash separation unit. In one device, the present invention realizes the viscosity breaking of the coal, devolatilization, gasification, fused ash separation and the cracking of tar and phenol, and has strong coal appropriateness for desulphurization in furnaces, and in addition, the device has the advantages of easy processing and production and simple operation control.
Description
The present invention relates to a kind of ash fusing fluidized bed coal gasification course and device thereof.
The coal gasification apparatus of Recent study exploitation both at home and abroad is broadly divided into three major types: high pressure fixed bed gasification (is representative with the Lurgi stove), entrained flow gasification (Texaco, Dow etc.) and pressurised fluidized bed gasification etc.The invention belongs to a kind of pressurization (or normal pressure) fluidized-bed gasification technology.
Fluidized-bed gasification can make vaporized material and vaporized chemical thorough mixing, helps heat transfer, mass transfer and gasification reaction, helps the utilization of pulverulent material, arranges the higher shortcoming of carbon loss in inferior and the flying dust but also brought simultaneously.Yan Jiukaifa fluidized-bed gasification afterwards is from the pre-treatment of ash discharge method (particularly adopting ash to contain intermingle with the method ash discharge), coal haply, flies time circulation and used heat utilizes several aspects to set about.
USP, 906,608 have just proposed a kind of dense fluidized bed gasification technology that adopts time melt polymerization ash discharge as far back as the end of the sixties, it is according to jet current principle, in the fluidized-bed bottom design tripping device of molten poly-ash, form a localized hyperthermia in the bed, make lime-ash reunion balling-up, by weight differential, reach separating of grey ball and carbonaceous material, thereby improved the carbon utilisation rate of raw material.Its primary structure is: in the bottom of dense phase fluidized bed conical grid distributor is arranged, its underpart connects the reducing pipe of a cone angle less than the former, and this pipe links to each other with the Venturi pipeline section, and Venturi tube and vertical sepn pipe join, at separator tube bottom suitable position, connect a horizontal vaporized chemical inlet pipe.Around described grid distributor, reducing pipe and Venturi tube, a cylindrical air chamber is arranged, the partial gasification agent enters fluidized-bed through air chamber.Control the gas speed of Venturi throat, can control the size or the weight of time ball.
USP4,057,402 has proposed a kind of fluidized-bed gasification process.This process is given processing with coal earlier: coal carries out the processing of giving of coal under 700-800 temperature in the fluidized-bed preprocessor; Coal after processed directly enters fluidized bed gasification reactor, adopt grey melt polymerization to get rid of lime-ash, flying time elder generation separates through the stove internal cyclone separators, the whirlwind separator separates outside stove again, circulation carbon containing flying dust returns gasification installation from molten poly-grey separator tube, in the preprocessor of coal, gives treatment temp for preventing coking and control, spray a considerable amount of water, waste heat boiler places the preprocessor of coal.Described gasification is set up the treatment unit that gives of coal, has increased the consumption of energy.Described flying dust circulation will be earlier through being in the stove internal cyclone separators under the condition of high temperature, so high to its material requirement, flying dust circulates by the separator of molten poly-ash, operates the control difficulty.Waste heat boiler is located in the preprocessor, reclaims the used heat of coal gas, and its scheme also may not be reasonable.
For the improvement of gasification installation, relate generally on the molten poly-grey isolating member, the essential features of the molten poly-isolation technique of ash or crucial inventive point are in Venturi throat structure, U.S. Pat P3,935,825; USP4,057,402; USP4,229,289; U5P4,369,45; USP4,023,280; USP4,191,539 grades have all adopted the Venturi throat structure, and the formation of these patents mainly is to change the structural parameter of Venturi tube or set up structures such as distribution plate or jet pipe therein, thereby makes operation or structure more complicated.
USP4,229,289 and USP4,554,375 introduced insert one in a kind of Venturi tube can aerating oxygen or the jet pipe of air so that cause the localized hyperthermia of fluidized-bed.It has still kept the Venturi throat that complex structure, processing and manufacturing bother.
First purpose of the present invention be to develop flying dust cyclical operation control that a kind of feed coal need not give processing easily, the method for the ash fusing fluidized bed gasifier bed gasification of waste heat recovery economical rationality.
Second purpose of the present invention is to design the ash fusing fluidized bed gasification installation that a kind of molten poly-ash discharge is simple in structure, waste heat recovery is controlled conveniently and had in the flying dust cyclical operation.
Gasification process of the present invention is formed by being equipped with coal, air feed, dedusting and five parts of waste heat recovery.The major equipment that this method relates to has rotary drying stove, vapourizing furnace, tornado dust collector, water-cooled eluting column, radiation and convection current waste heat boiler.Described being equipped with in the coal process, do not need coal broken in advance sticking.
The technological process of the molten dimerization bed gasification of ash is as follows:
The feed coal of experiment usefulness is sent into the coal canopy through automobile, behind rotary conveyor, tramp iron separator, send into double roll crusher then, coal after the fragmentation is through screening, send into the rotary drying stove less than the coal of 6mm, be dried to moisture content＜5%, it is standby to send into coal bunker through embedded scraper transporter again, and the coke powder that is used for experimentation is also with the same manner preparation and be stored in coke bin.In process of the test, coke powder or coal are delivered to the metering coal bunker through vibro-feeder, chapelet, coal bunker in the middle of entering after the electronic scales metering, coal bunker in the middle of entering after boosting, stably enter feed-pipe thus, send into vapourizing furnace with strength through screw feeder.
Each experiment at first uses the diesel oil baker to 800-1000 ℃, starts feeding screw then, controls certain inlet amount, and adjusting air, steam flow bring into operation.The coal gas that process generates is carried the part fine powder secretly and is entered one-level and secondary cyclone through (its temperature is reduced to about 750 ℃) behind the radiation waste-heat boiler, captured and returned vapourizing furnace concentrated phase section at this most of fine powder and further burn, gasify through corresponding riser systems, so that carry the high-carbon transformation efficiency, the fine powder internal circulating load is controlled by the driven plate valve.The coal gas that carries a small amount of fine powder enters convection type waste heat boiler and shell and tube air preheater, and gas temperature is reduced to and entered water-cooled pouring washing tower about 170 ℃, further exports behind cooling and the depositing dust.The steam that waste heat boiler produced is except that a part is personal, most of output, the used air of process enters gas distributor, jet pipe and grey separator tube from compressor through (about 150 ℃) Fen Sanlu after the preheating, to guarantee that fluidisation, gasification and ash content are from the carrying out of process in the stove.
Mass flow in this process, pressure, temperature and weight are used measurements such as orifice-plate flowmeter, pressure (pressure reduction) transmitter, thermocouple thermometer, electronic scales respectively, and signal is all sent into the super small-sized collecting and distributing control system of μ XL of Japanese Yokogawa Motor company and handled, controls, shows, prints.
Coal gas in the experimentation is formed gas chromatograph (GC-RIA) timing analysis of adopting day island proper Tianjin company, and the ash discharge carbon content adopts the CR-12 carbometer of U.S. LECO company to measure, and water analysis entrusts Taiyuan City environment monitoring portion to measure by national standard method.
The structure of described ash fusing fluidized bed vapourizing furnace is as follows:
This device by molten poly-ash content from the unit, the fluidized-bed gasification unit, fly time cycling element and four parts of waste heat recovery unit are formed.
Described molten poly-ash content is made of conical grid distributor, conical reducing pipe, vertical sepn pipe and horizontal inlet pipe thereof, cylindrical air chamber and horizontal vaporized chemical inlet pipe thereof and central jet pipe (oxygenant inlet pipe) from the unit, it is characterized in that, the vertical sepn pipe directly links to each other with reducing pipe, has saved the Venturi pipeline section of complex structure, processing difficulties.Described flying dust partitioning cycle unit is made of the outer whirlwind separator of stove, vertical circulation tube, differential pressure monitor, grey internal circulating load variable valve and air conveying institute.Carry secretly and fly inferior coal gas earlier through deriving from the gasification furnace roof after the exhaust heat recovery apparatus cooling in the stove, through cyclonic separation, raw gas advances purification system, and flying dust advances all vertical circulation tube down by cyclonic separator, enters the fluidized-bed gasification unit through variable valve and pneumatic carrier.
Exhaust heat recovery apparatus in the described vapourizing furnace is the shell and tube boiler systems.
Described fluidized-bed gasification unit is by the close phase of bottom, and fluidisation section and upper extension section are formed, and original thing and recycle stock directly enter close phase section.
Gasification process of the present invention and major equipment accompanying drawings thereof are as follows.
Fig. 1 is the Unit of Coal Gasification for Pulverized Coal with Ash schema
Fig. 2 is ash fusing fluidized bed gasification installation overall structure synoptic diagram
Fig. 3 is for melting poly-ash content from cell schematics
Fig. 4 is the grid distributor schematic top view
Fig. 5 is for melting poly-ash content from the unit schematic partial sectional view
Gasification furnace structure as shown in the figure, the fluidized-bed gasification unit is made of body of heater 1, top expanding reach 17, feed-pipe 9, dense fluidized section 16; Exhaust heat recovery apparatus is made of shell and tube boiler 8 in the stove; Flying time partitioning cycle unit is made of gas pipe 15, differential pressure meter 6, vertical circulation tube 19, flying dust internal circulating load variable valve 7, pneumatic carrier 14; Molten poly-ash content is made of conical grid distributor 2, reducing pipe 3, central jet pipe 4, vertical separator tube 5, cylindrical air chamber 18, vaporized chemical inlet pipe 12,10 and 11, row's time pipe 13 from the unit.
The angle that take out at the element of cone of described grid distributor and center is 45 degree, and the hole on the grid distributor 16 is circular.
The element of cone of described reducing pipe and the angle of central shaft are the 10-25 degree.
The equipment of gasification is as shown in the figure:
21 is rotary conveyor, and 22 for burying scraper plate, and 23 is rotary dryer, 24 is coal bunker or coke bin, and 25 is bucket elevator, and 26 is coal, 27 is vapourizing furnace, 28 is ash bucket, and 29 is the I and II cyclonic separator, and 30 is waste heat recovery, 31 is air preheater, 32 is water wash column, and 33 is feeding screw, and 34 is crusher.
The characteristics of ash fusing fluidized bed gasification installation are as follows:
(1) in this single device, realized the cracking of broken sticking, devolatilization, gasification, grey reunion and separation, tar and the phenols of coal.
(2) the vaporized chemical water vapor enters gasification section from grid distributor, makes the grid distributor place keep certain oxygen concn, forms relative cold zone, has prevented ash erosion effectively.
(3) part oxygen or air spray into the gasification zone from the center jet pipe, make to form a localized hyperthermia in the stove, impel grey reunion balling-up, impel ash effectively to separate with coal, have improved the utilization ratio of carbon.
(4) set up flying dust partitioning cycle unit, the carbon in the flying dust is further gasified, improved the utilization ratio of carbon.
(5) coal gas of high temperature produces steam as vaporized chemical earlier through waste heat recovery, also can be used for the heat of giving of air or oxygen then, has improved the overall thermal efficiency of process.
(6) test-results shows, the coal adaptability of this device wide (coke, hard coal, bituminous coal and low grade coal etc.), gasification intensity height (3-10 of fixed bed is doubly), and service temperature is moderate.
(7) can simplify gas cleaning system at desulfuration in furnace to high sulphur coal.
(8) do not contain tar in the product gas, it is low to contain the phenol amount.
In addition, the processing and manufacturing of this device is easy, and operation control is simple.
Test-results of the present invention and similar stove relatively list in table 1.The character and the test-results thereof of the different coals of the present invention are listed in table 2 and table 3.The representative result of the similar type of furnace research of table 1. aspect
U.S. U.S. U.S. China China
IGT IGT KRW Shanxi Shanxi coalification institute of coalification institute
Internal diameter: 09 internal diameter: 0.9 external diameter, 1.2 internal diameters: 1.0 internal diameters: 1.0 gasification furnace size m height: 76 height: 7.6 height: 15 height: 14 height: 14 gasifying agents air-steam oxygen-steam air-steam air-steam oxygen-steam coal input quantity Kgh 281-359 438-859 500-780 500-1050 500-1000 reaction control temperature ℃ 950-1200 1011-1032 760-1040 1060-1100 1085-1095 gasification furnace pressure MPa 0.16-0.39 0.078-0.13 0.98-1.67 0.1-0.3 0.035-0.18 ash discharge carbon content % 5-30＜10 5-25＜10 efficiency of carbon con version % 70-98 74.9-89.7 70-90＞80 air/coal Kg/Kg 2.80-3.25 2.49-4.33 3.48-4.26 steam/coal Kg/Kg 0.46 0.83 0.28-1.58 0.2-0.5 0.45-0.65 1.20-1.40 oxygen/coal Kg/Kg 0.19-0.77 0.75-0.89 composition of coal gas V%
CO 14.55-20.50 23.8-33.9 16.2-21.5 10.21-15.38 22-28
CO
2 9.0-10.9 21.0-28.8 13.4-16.9 11.81-16.72 24-35
CH
4 0.21-1.0 2.5-5.7 1.2-2.2 0.86-1.68 1.3-2.3
H
2 9.47-17.50 39.9-43.0 11.4-1 1.9 12.14-21.42 40-46
N
252.9-63.9 51.6-53.3 54.16-60.79 caloric power of gas (HHV) DJ/Nm
34436-4585 9305-11046 4195-4375 3912-4548 8727-10227 table 2. gasified raw material analytical data
Table 3. model experiment result
| Raw material | Coke is washed middle coal lean coal bottle coal |
| Worker M adIndustry A adDivide V adAnalyse characteristic of char residue Wt% | 1.42 1.53 0.68 4.42 24.14 41.36 21.25 5.99 2.16 18.49 14.85 32.15 1 4 5 3 |
| The C of unit adPlain H adDivide O adAnalyse N ad Wt％ S tad | 70.57 45.92 67.51 73.98 2.21 2.97 3.56 4.46 1.21 7.03 2.82 9.70 0.46 0.74 0.97 1.24 0.99 0.45 3.21 0.21 |
| FT ℃ of the molten ST point of ash DT | ＞1500 ＞1500 1500 1200 ＞1500 ＞1500 ＞1500 1220 ＞1500 ＞1500 ＞1500 1240 |
| Calorific value Q netV_ ad MJ/kg | 24.84 23.71 27.10 29.34 |
| Ash SiO 2 Al 2O 3Group Fe 2O 3CaO becomes MgO TiO 2 Wt％ SO 3 K 2O Na 2O P 2O 5 | 50.50 49.11 45.36 49.39 35.97 39.07 33.70 14.25 6.97 5.02 13.08 4.77 2.42. 2.29 3.13 29.71 0.71 0.62 0.71 2.26 0.67 1.59 1.28 0.83 1.15 0.45 0.75 3.00 - 1.15 0.35 0.88 - 0.10 0.10 1.00 - 0.20 - 0.92 |
Lean coal lean coal bottle coal is washed middle coal lean coal lean coal gasifying agent air-steam air-steam air-steam air-steam oxygen-steam oxygen-steam coal input quantity Kg/h 640 1,021 474 529 518 1080 reaction control temperature ℃ 1,100 1,081 1,068 1,080 1,090 1085 gasification furnace pressure KPa, 251 300 40 22 36 153 ash discharge carbon content %, 3.41 9.92 19.46 17.82 8.03 32.68 efficiency of carbon con version %, 87.7 82.9 83.4 79.19 83.1 91.8 air capacity Nm3,1,848 2,787 1,271 1096 quantity of steam Kg/h, 331 500 193 150 600 1296 amount of oxygen Nm3/ h 261 498 coal factor of created gase Nm
3/ kg 3.96 3.77 3.74 2.70 2.16 2.21 coal gas are formed V%
CO 15.34 15.03 14.49 11.70 22.65 27.10
CO
2 11.21 11.28 11.28 12.60 27.00 25.54
CH
4 1.35 1.41 0.80 0.07 1.32 2.23
H
2 14.32 14.85 16.57 13.79 35.25 37.42
N
257.77 57.43 56.86 51.04 13.77 7.70 caloric power of gas (HHV) KJN/m
34,298 4,350 4,261 856 7,871 9066
Claims (4)
1. ash fusing fluidized bed gasification process, it is formed by being equipped with coal, air feed, gasification, dedusting and five parts of waste heat recovery, it is characterized in that the described coal part that is equipped with constitutes by pulverizing with dry two steps, need pre-broken the gluing of coal, broken coal is sent into the rotary drying stove through sieving less than the coal of 6mm, drying obtains the coal of moisture content＜5%, control certain inlet amount, regulate air, steam flow is sent into gasification in the stove; The dust-laden coal gas that generates reclaims heat through the radiation waste heat boiler and enters a secondary cyclonic separation dedusting; The coal gas that carries a small amount of fine powder gives hot device and water-cooling tower through shell and tube waste heat boiler, air and further lowers the temperature and export after the dedusting.
2. a kind of ash fusing fluidized bed gasification installation in the gasification process according to claim 1, constitute from the unit by fluidized-bed gasification unit and molten poly-ash content, described molten poly-ash content from the unit by conical grid distributor, conical reducing pipe, vertical sepn pipe and horizontal vaporized chemical inlet pipe thereof, cylindrical air chamber and horizontal vaporized chemical inlet pipe thereof and central jet pipe constitute, it is characterized in that described vertical sepn pipe directly links to each other with conical reducing pipe, the flying dust partitioning cycle unit of setting up is by the outer whirlwind separator of stove, vertical circulation tube, flying dust internal circulating load variable valve, the pressure reduction monitor, pneumatic carrier is formed.
3. gasification installation as claimed in claim 2 is characterized in that the conical bus of described grid distributor and the angle of axis are 45 degree, and the pore on the grid distributor is circular.
4. gasification installation as claimed in claim 2 is characterized in that the angle of conical bus of described reducing pipe and central shaft is the 10-20 degree.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94106781A CN1038846C (en) | 1994-07-02 | 1994-07-02 | Gasification process and device of ash fusing fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94106781A CN1038846C (en) | 1994-07-02 | 1994-07-02 | Gasification process and device of ash fusing fluidized bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1114976A CN1114976A (en) | 1996-01-17 |
| CN1038846C true CN1038846C (en) | 1998-06-24 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN94106781A Expired - Lifetime CN1038846C (en) | 1994-07-02 | 1994-07-02 | Gasification process and device of ash fusing fluidized bed |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101457160B (en) * | 2009-03-06 | 2011-06-08 | 安徽淮化集团有限公司 | Entrained flow coal gasification method employing solid state slag-tap suitable for high ash content and high ash melting point coal |
| CN102242005A (en) * | 2010-05-14 | 2011-11-16 | 中国石油化工集团公司 | Coal gasification device utilizing coal melting collection and high-temperature waste heat recovering method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US419539A (en) * | 1890-01-14 | Steam blower and drier for furnaces | ||
| US4057402A (en) * | 1976-06-28 | 1977-11-08 | Institute Of Gas Technology | Coal pretreatment and gasification process |
| US4229289A (en) * | 1979-03-12 | 1980-10-21 | Institute Of Gas Technology | Fluidized bed apparatus and process |
| CN1083851A (en) * | 1992-05-08 | 1994-03-16 | 维多利亚州电力委员会 | The drying of integrated carbonaceous fuel and the method and apparatus of gasification |
-
1994
- 1994-07-02 CN CN94106781A patent/CN1038846C/en not_active Expired - Lifetime
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US419539A (en) * | 1890-01-14 | Steam blower and drier for furnaces | ||
| US4057402A (en) * | 1976-06-28 | 1977-11-08 | Institute Of Gas Technology | Coal pretreatment and gasification process |
| US4229289A (en) * | 1979-03-12 | 1980-10-21 | Institute Of Gas Technology | Fluidized bed apparatus and process |
| CN1083851A (en) * | 1992-05-08 | 1994-03-16 | 维多利亚州电力委员会 | The drying of integrated carbonaceous fuel and the method and apparatus of gasification |
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| CN1114976A (en) | 1996-01-17 |
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