CN1405277A - Solid slag-discharing dry-powder air-current bed gasification process and apparatus - Google Patents
Solid slag-discharing dry-powder air-current bed gasification process and apparatus Download PDFInfo
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Abstract
There is a kind of gasifying method and device for new solid sediment-discharging dried powder flowing bed. The method is made up of six sections which are preparing coal, providing steam, gasifying, sediment-eliminating, cleaning dust and waste heat reclaiming. The cola is divided into two sections of coal flour small than 8mm and power coal small than 0.09mm. The device is made up of melted dust separating unit, gasifying unit. The invention realizes the combination of the high-temperature flow bed gasification, the semi carbon and coal gas the flowing bed cools the high-temperature sediment and gases which is generated by the flowing bed.
Description
Affiliated field: the invention belongs to a kind of air-current bed gasification process and device, relate in particular to a kind of solid slag-discharing dry-powder air-current bed gasification process and device thereof.
Background technology:
On current domestic and international Coal Gasification Technology development trend, maximizing, pressurize, adapt to multiple fine coal, low pollution, easily purifying is the gasification developing direction.External vapourizing furnace newly developed mainly adopts high temperature, pressure gasification process, and its advantage is: improve gasification intensity; Single furnace output height; Adapt to multiple coal dust.The external existing pressurized gasification type of furnace mainly is divided three classes: and pressurization static bed vapourizing furnace (as the Lurgi stove), pressurized fluidized bed gasifier (HTW) and pressurized air flow bed gasification furnace (Texaco, DOW, Shell, Prenflo).This three classes vapourizing furnace respectively has its advantage, and industrialization level is the most ripe with Shandong strange (Lurgi), Texaco (Texaco), and Shell, Prenflo have also finished the demonstration plant exploitation, and day output reaches 400～2500 tons magnitude.The pressurization static bed vapourizing furnace of Lu Qi is a raw material with weak bonding lump coal, and cold gas efficiency is the highest, but purification system complexity (tar processing); It is raw material that Texaco gasifier needs with low ash, low-ash-fusion coal, high-temperature operation, and gasification intensity and GAS QUALITY are higher, but the oxygen consumption is high, facility investment is high; The Shell gasification technology of dry powder charging increases by two percentage points than Texaco gasification technology gasification efficiency, in recent years, air flow bed dry feed gasification technology is wide because of adaptability to raw material, cold gas efficiency is high, efficiency of carbon conversion is high, separate unit throughput height is paid attention to by people.
Existing in the world at present several dry-powder air-current bed gasification flow process is close: raw coal is through pulverizing, be dried to suitable water-content (as: brown coal 8%～10%, bituminous coal 1%～2%), granularity is less than 0.1mm, go into normal pressure coal bunker and pressurization coal bunker, (coal dust: vapourizing furnaces are imported in delivering gas=20～30kg/kg) to fine coal by the pneumatic conveyor system concentrated phase with nitrogen.Vapourizing furnace is provided with installs symmetrical burner, steam, oxygen and coal dust in the reaction in furnace temperature above 1370 ℃.Most of ash content is dissolved in the thermal-flame district in the coal, and is dirty along the gasification furnace wall with the form of slag, enters the slag water-bath and solidifies, granulates, and discharges gasification system by ash hoist, grey lock hopper.Raw gas contains a spot of fusion ash that does not burn carbon and a great deal of, before entering waste heat boiler, utilizes the Quench method that raw gas is cooled to below 1100 ℃ usually, to avoid the viscosity lime-ash to enter waste heat boiler and to be bonded on the boiler tube wall.Coal gas goes out after the waste heat boiler, enters dedusting and water wash system, removes most dusts, and gas temperature is cooled to 35 ℃ simultaneously.
The very big characteristics of entrained flow gasification are that the coal grain can be separated by air-flow separately, and fuel pellet is difficult in the plastic stage cohesion, thereby the cohesiveness of fuel is to not influence of gasification.Coal dust and vaporized chemical carry out and gasization, and the speed of relative movement between the reactant is little, and duration of contact is short.In order to improve speed of response, be vaporized chemical generally, and grind coal dust very thin with pure oxygen steam, increase the reaction table area; For carbon is transformed fully, must improve temperature of reaction, furnace temperature is generally than the high 100-150 of ash fusion point ℃, and therefore, ash content is discharged with molten state usually, also must be noted that the viscosity-temperature characteristics of ash content when selective combustion.Because gasification reaction is to carry out, must consider the high temperature material of vapourizing furnace under the condition of high temperature.
The K-T stove adopts the pressurization spraying to contain the chromium refractory concrete at present, once is sprayed into, and the life-span can reach 3-5, and slag is mobile to be corroded but the Lower Half of lining is because of having, and is easy to damage; Shell and GSP vapourizing furnace have adopted membrane wall, have increased the work-ing life of refractory brick, but because complicated water wall, dross technology and slag tap system, equipment manufacturing cost is higher; The Prenflo inner lining refractory block, it is outer to be steam jacket, top is waste heat boiler.K-T stove and GSP adopt the method for water Quench to reduce the raw gas temperature out, and Shell vapourizing furnace and Prenflo vapourizing furnace then adopt the way of circulation cooled coal gas Quench.
According to coal gasification reaction thermodynamic(al)equilibrium and dynamic analysis, in 1200 ℃～1300 ℃ temperature ranges, coal gasification reaction can carry out fully, reaches maximum trim point.And at present in the world entrained flow bed gasification technology all adopts temperature operation more than 1400 ℃, its objective is and realizes slag tap in order to increase the flowability of melt cinder.But the liquid film of melt cinder is unfavorable for the diffusion of gasifying medium, influences efficiency of carbon conversion; Too high temperature causes oxygen consumption height, cold gas efficiency reduction, refractory materials to require height.In addition, based on CO, disproportionation taking place easily in the present existing dry-powder air-current bed gasification gas, is unsuitable for the synthetic demand of existing chemical industry; Slag tap need be set up slag crusher, and wants strict controlled chilling tank temperature, water treatment system complexity; Gas outlet temperature is too high, the Waste Heat Recovery System (WHRS) costliness; Refractory brick life is short, and adopts film water cold wall structure complexity, costliness; Coal handling system is huge, power consumption is high; The characteristic of the high ash of CHINESE COAL, high ash melting point more is unfavorable for the slag tap entrained flow gasification.
First purpose of the present invention provides a kind of simple to operate, long service life, the method for the dry ash extraction dry method entrained flow gasification that running cost is low.
Second purpose of the present invention is to design a kind of simple in structure, the solid slag-discharing dry-powder air-current bed gasification installation that cost is low.
The present invention combines air flow bed with the fluidized-bed gasification process, the dry coal powder gasifies under air flow bed section hot conditions, the molten ash that produces is carried with coal gas of high temperature and enters fluidized-bed and the air flow bed section of crossing, and rapidly with fluidized-bed in " low temperature " semicoke mix with " low temperature " coal gas that is produced.The fused lime-ash is cooled into solid slag to be mixed with semicoke, and selectively is discharged from vapourizing furnace from system with solid-state form by the molten poly-ash content of fluidized-bed bottom.
The method of solid slag-discharing dry-powder air-current bed gasification of the present invention comprises the steps:
(1). the preparation of gasified raw material coal
Through screening, be dried to moisture content＜5wt% less than the coal of 8mm after the feed coal fragmentation, a part of exsiccant broken coal is sent into the broken coal storehouse, as the fluidized-bed gasification raw coal; Another part broken coal is crushed to less than 0.09mm again, sends into the fine breeze coal bunker, as the entrained flow gasification raw coal;
(2). gasification
A. at first vapourizing furnace is carried out baker, treat vapourizing furnace bottom and air flow bed middle part temperature greater than 900 ℃, head temperature is during greater than 400 ℃, bubbling air, steam and broken coal bottom fluidized-bed, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal are operated than 0.3～0.6kg/kg;
B. treat the quiet bed height and the bed equal diameters of semicoke material in the fluidized-bed concentrated phase section, switch to oxygen/humidified blast after system operation is stable, temperature is controlled at 800～900 ℃ in the handoff procedure;
C. press the oxygen coal than 0.4～0.5Nm
3/ kg, steam coal are operated than 0.5～1.0kg/kg, and temperature-stable is 900～1100 ℃ of scopes;
D. behind the fluidized-bed part system stability, particle diameter is delivered to the coal-fired nozzle of air flow bed less than the dry coal powder of 0.09mm by the fine breeze coal bunker,, presses oxygen dry coal powder than 0.5～0.7Nm again to coal-fired nozzle aerating oxygen and steam
3/ kg, steam coal are operated than 0.1～0.3kg/kg, and air flow bed part operation temperature is 1200～1400 ℃ of scopes.Fluidized-bed and the air flow bed section of crossing and top expanding reach temperature are 1150～1300 ℃ of scopes.
(3). the deslagging of vapourizing furnace
In gasification, regulate ring pipe gas speed at 5～10m/s, oxygen concn＜25Vol.%; Central jet pipe gas speed 10～30m/s, oxygen concn 40～60%vol.%, control bed drain purge;
(4). the purification of raw gas and waste heat recovery
Add chilled water steam or heat recovery system in the vapourizing furnace outlet, assurance vapourizing furnace temperature out＜900 ℃.Raw gas separates through cyclonic separator, and the semicoke fine powder of capture participates in reaction once more through charging feed fine breeze transfer pot such as semicoke fines collection/cooling tank, fine powder delivery systems; Through waste heat boiler, interchanger, gas temperature is reduced to and is entered the water-cooled eluting column about 170 ℃ through the coal gas of high temperature of roughing out, further exports after cooling and the dedusting;
5. vapourizing furnace stops
During orderly shutdown, at first cut off entering back system gas line, coal gas emptying; The coal-fired nozzle oxygen of closed gas flow bed is closed coal-fired nozzle stem coal dust again, opens the giant quantity of steam simultaneously, plays the effect that protection nozzle, purging and air flow bed are partly lowered the temperature; Afterwards, reduce fluidized-bed ring pipe gas speed and strengthen the ash discharge amount, strengthen the fluidized bed steam consumption simultaneously, close oxygen valve, close the broken coal of fluidized-bed, temperature is controlled at below 900 ℃ in the stove.After furnace charge has been arranged, stop air inlet, final system is used steam, air purge one time respectively.
A kind of simple in structure in order to realize that the present invention designs, the special-purpose solid slag-discharing dry-powder air-current bed gasification installation that cost is low.
Solid slag-discharing dry-powder air-current bed gasification installation of the present invention by molten poly-ash content from the unit, solid slag-discharing dry-powder air-current bed gasification unit and waste heat recovery unit form, the described molten ash content that gathers is made of circular cone grid distributor, reducing pipe, central jet pipe, vertical separator tube, cylindrical air chamber, vaporized chemical inlet pipe from the unit; Described waste heat recovery unit is made of the shell and tube boiler; Described solid slag-discharing dry-powder air-current bed gasification unit is by the fluidized-bed gasification section of bottom, jet fluidized bed gasification section and upper extension section are formed, to jet fluidized bed gasification section by two dry-powder air-current bed reacting cylinder body of symmetry, fine breeze combustion mouth, vaporized chemical inlet pipe and fine breeze concentrated phase transfer lime constitute.The angle β of the element of cone of described grid distributor and central shaft is 20～50 degree, and the hole on the grid distributor is circular.
The angle γ of the element of cone of described reducing pipe and central shaft is the 5-20 degree.
Described is 0～30 degree to spray powder air flow bed central shaft and the axle clamp angle α of vertical reactor main center, and two central shaft point of contacts are apart from fluidized-bed sparger upper edge height L=0.5-2D, and D is a fluidized-bed concentrated phase section diameter.The present invention compared with prior art has following advantage:
1). realize that dry cinder discharging saves the chilled water treatment system with the cold slag of Jiao;
2). " low temperature " operation, vapourizing furnace body temperature replace the circulation cooled coal gas at 1100～1300 ℃ with low temperature coal gas, reduce the oxygen consumption, improve cold gas efficiency;
3). make full use of sensible heat, coal gas and hot grey sensible heat are used for coal gasification reaction;
4). regulate CO and H in the coal gas
2Ratio, it is synthetic to meet chemical industry;
5). structure of reactor is simple, no special refractory, cost is low;
6). the coal ash characteristic is required to relax,, adapt to most of CHINESE COAL characteristics according to the coal characteristic attemperation;
7). can directly use the part broken coal, reduce the coal-grinding power consumption.
8). simple to operate, long service life.
Embodiment:
Gasification process of the present invention and specific equipment accompanying drawings thereof are as follows:
Fig. 1 is novel solid slag-discharing dry-powder air-current bed coal gasification schema
Fig. 2 is novel solid slag-discharing dry-powder air-current bed gasifying powder coal device structural representation
Fig. 3 is for melting poly-ash content from cell schematics
Embodiment 1: as shown in the figure, solid slag-discharing dry-powder air-current bed gasification unit is by body of heater 1, insulation material 2 and refractory material 3, top expanding reach 20, and dense fluidized section 17, to spray powder air flow bed 18, broken coal feed pipe 12 and fine breeze nozzle 15 consist of; Exhaust heat recovery apparatus is made of shell and tube boiler 16 in the stove; Molten poly-ash content is made of circular cone distribution grid 4, reducing pipe 5, central jet pipe 6, vertical separator tube 8, cylindrical air chamber 7, gasifying agent air inlet pipe 9,10 and 11 from the unit; By two dry-powder air-current bed reacting cylinder body 18 of symmetry, fine breeze fires mouth 15 to spray powder air flow bed unit, and gasifying agent air inlet pipe 14 and fine breeze concentrated phase carrier pipe 13 consist of. 21 is belt conveyor, and 22 is disintegrating machine, and 23 for burying scraper plate, 24 is vibrating sieving machine, and 25 is rotary dryer, and 26 is vibrating sieving machine, 27 are winnowing type pulverizing and separator, and 28 is the fine powder vibrating sieving machine, and 29 for burying scraper plate, 30 is dried fine powder warehouse, and 31,32 is concentrated phase pneumatic transporting tank sending, and 33 for burying scraper plate, 34 is the broken coal warehouse, and 35 is oscillating feeder, and 36 is bucket elevator, 37,38,39 is the broken coal feeding warehouse, and 40 is feeding screw, and 41 is gasification furnace, 42 is ash bucket, and 43 is the I and II cyclone separator, and 44 is the flying dust cooler, 45 is the circularly-supercharged tank of flying dust, and 46 is Waste Heat Recovery, and 47 is air preheater, 48 is water scrubber, and 49 is the gasifying agent sub-cylinder, and 50 is raw coal, 51 is boiler soft water, and 52 is steam, and 53 is circulation cleaning water, 54 is coal gas, and 55 is air, and 56 is water vapour, 57 is oxygen, and 58 is lime-ash.
Respectively Shaanxi Bin County raw coal is crushed to granularity less than the broken coal of 8mm with less than the fine breeze of 0.09mm, the coal bunker 34 and 30 of packing into after the drying is stand-by. Heating makes fluidized gasification furnace bottom 17 temperature and spray powder air flow bed body of heater 18 temperature is reached 900 ℃, and top of gasification furnace 20 temperature reach 400 ℃. Open the air/steam blower system and advance coal feeding screw 40, raw coal is added in the gasification furnace 41 coal input quantity 40kg/h, air capacity 120Nm via coal bunker 393/ h, quantity of steam 20kg/h. Set up behind the bed when temperature, pressure, flow system all reach and switch to oxygen/steam blast, oxygen feeding amount 20Nm after imposing a condition3/ h, water vapour amount 37kg/h, temperature is controlled at about 800～900 ℃ in the handoff procedure, then slowly regulates oxygen, steam flow, guarantee flow velocity, oxygen concentration that distributor 4, endless tube 8 and central jet pipe 6 need, end temperature is stabilized in the set point value of 900～1100 ℃ of scopes.
Behind the system stability, open fine powder delivery system 31 or 32, after guaranteeing that fine breeze is normal and carrying, open 14, two total fine powder amount 60kg/h of symmetrical air flow bed of nozzle vaporized chemical inlet pipe, amount of oxygen 36Nm
3/ h, quantity of steam 8kg/h, the air flow bed portion temperature is brought up to 1300～1400 ℃ of scopes, stable operation gradually by 900 ℃.After air flow bed is partially stabilized, by regulating fluidized-bed gasification section gasification dosage and broken coal coal input quantity control fluidized-bed and the air flow bed section of crossing and top expanding reach temperature to required value.Oxygen is 0.5Nm with the ratio of broken coal
3/ kg, oxygen is 0.6Nm with the fine breeze ratio
3/ kg, the ratio of water vapor broken coal is 0.925kg/kg, water vapor is 0.133kg/kg with the fine breeze ratio.The vapourizing furnace section of crossing temperature is controlled at 1214 ℃
Lime-ash in the vapourizing furnace 41 enters in the ash bucket 42 through the vapourizing furnace bottom, regularly discharges lime-ash from ash bucket 42.In operational process, by suitably adding chilled water steam at outlet of still, assurance vapourizing furnace temperature out＜900 ℃.Raw gas separates 43 through cyclonic separator, and the semicoke fine powder of capture participates in reaction once more through fine powder recycle system charging feed fine breeze transfer pot 31 or 32 such as semicoke fines collection and cooling tank 44, fine powder delivery systems 45; Through waste heat boiler 46, interchanger 47, gas temperature is reduced to and is entered water-cooled eluting column 48 about 170 ℃ through the coal gas of high temperature of roughing out, further exports after cooling and the dedusting.The used vaporized chemical of process (oxygen, steam) each minute 4 tunnel enters fluidized-bed lime-ash cooling bath gas distributor 7, jet pipe 6, ash content from organ pipe 8 and the coal-fired nozzle 15 of air flow bed, to guarantee gasification in the stove, fluidisation, slag cooling and ash content the carrying out from process.
Embodiment 2: fluidized-bed part broken coal coal input quantity 42kg/h, oxygen feeding amount 21Nm
3/ h, water vapor amount 38kg/h; The total fine powder amount 43kg/h of air flow bed, amount of oxygen 26Nm
3/ h, quantity of steam 6kg/h; The vapourizing furnace section of crossing temperature is controlled at 1173 ℃, and all the other are with embodiment 1.
Embodiment 3: fluidized-bed part broken coal coal input quantity 40kg/h, oxygen feeding amount 21Nm
3/ h, water vapor amount 38kg/h; The total fine powder amount 100kg/h of air flow bed, amount of oxygen 59Nm
3/ h, quantity of steam 15kg/h; The vapourizing furnace section of crossing temperature is controlled at 1255 ℃, and all the other are with embodiment 1.
Embodiment 4: fluidized-bed part broken coal coal input quantity 42kg/h, oxygen feeding amount 21Nm
3/ h, water vapor amount 39kg/h; The total fine powder amount 170kg/h of air flow bed, amount of oxygen 102Nm
3/ h, quantity of steam 25kg/h; The vapourizing furnace section of crossing temperature is controlled at 1302 ℃, and all the other are with embodiment 1.
List in table 1 as the novel solid slag-discharing dry-powder air-current bed gasification preparing synthetic gas gas composition of carrying out under the embodiment 1-4 condition.
Novel solid slag-discharing dry-powder air-current bed gasification preparing synthetic gas gas composition under table 1 different condition
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Total coal input quantity kg/h | ????100 | ????85 | ????140 | ????212 |
| Total oxygen feeding amount Nm 3/h | ????56 | ????47 | ????80 | ????123 |
| Total quantity of steam kg/h | ????44 | ????45 | ????53 | ????64 |
| The oxygen coal compares Nm 3/kg | ????0.560 | ????0.553 | ????0.571 | ????0.580 |
| Steam coal compares kg/kg | ????0.45 | ????0.529 | ????0.379 | ????0.302 |
| Hybrid reaction temperature ℃ | ????1214 | ????1173 | ????1255 | ????1302 |
| Dry gas is formed Vol.% | ||||
| CO2 | ????11.430 | ????9.68 | ????7.923 | ????5.985 |
| H2 | ????37.009 | ????35.86 | ????34.737 | ????33.481 |
| CO | ????46.673 | ????49.63 | ????52.597 | ????55.870 |
| CH4 | ????0.728 | ????0.59 | ????0.457 | ????0.307 |
| N2 | ????4.025 | ????4.09 | ????4.156 | ????4.229 |
| Factor of created gase Nm 3/kg | ????2.04 | ????2.05 | ????2.03 | ????2.02 |
| Caloric power of gas Kcal/Nm3 | ????2610.88 | ????2652.77 | ????2694.87 | ????2741.28 |
| Efficiency of carbon conversion % | ????99 | ????99 | ????99 | ????99 |
| Cold gas efficiency % | ????82.41 | ????82.24 | ????82.08 | ????81.90 |
Claims (5)
1. a solid slag-discharing dry-powder air-current bed gasification process is made up of the purification and the waste heat recovery that are equipped with coal, gasification, deslagging, raw gas, it is characterized in that:
(1) preparation of gasified raw material coal
Through screening, be dried to moisture content＜5wt% less than the coal of 8mm after the feed coal fragmentation, a part of exsiccant broken coal is sent into the broken coal storehouse, as the fluidized-bed gasification raw coal; Another part broken coal is crushed to less than 0.09mm again, sends into the fine breeze coal bunker, as the entrained flow gasification raw coal;
(2) gasification
A. at first vapourizing furnace is carried out baker, treat vapourizing furnace bottom and air flow bed middle part temperature greater than 900 ℃, head temperature is during greater than 400 ℃, bubbling air, steam and broken coal bottom fluidized-bed, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal are operated than 0.3～0.6kg/kg;
B. treat the quiet bed height and the bed equal diameters of semicoke material in the fluidized-bed concentrated phase section, switch to oxygen/humidified blast after system operation is stable, temperature is controlled at 800～900 ℃ in the handoff procedure;
C. press the oxygen coal than 0.4～0.5Nm
3/ kg, steam coal are operated than 0.5～1.0kg/kg, and temperature-stable is 900～1100 ℃ of scopes;
D. behind the fluidized-bed part system stability, particle diameter is delivered to the coal-fired nozzle of air flow bed less than the dry coal powder of 0.09mm by the fine breeze coal bunker,, presses oxygen dry coal powder than 0.5～0.7Nm again to coal-fired nozzle aerating oxygen and steam
3/ kg, steam coal are operated than 0.1～0.3kg/kg, and air flow bed part operation temperature is 1200～1400 ℃ of scopes.Fluidized-bed and the air flow bed section of crossing and top expanding reach temperature are 1150～1300 ℃ of scopes.
(3) deslagging of vapourizing furnace
In gasification, regulate ring pipe gas speed at 5～10m/s, oxygen concn＜25Vol.%; Central jet pipe gas speed 10～30m/s, oxygen concn 40～60%vol.%, control bed drain purge.
2. a kind of device of solid slag-discharing dry-powder air-current bed gasification process according to claim 1, it is characterized in that by molten poly-ash content from the unit, solid slag-discharing dry-powder air-current bed gasification unit and waste heat recovery unit form, described molten poly-ash content from the unit by circular cone grid distributor (4), reducing pipe (5), central jet pipe (6), vertical separator tube (8), cylindrical air chamber (7), vaporized chemical inlet pipe (9,10,11) constitute; Described waste heat recovery unit is made of shell and tube boiler (16); Described solid slag-discharing dry-powder air-current bed gasification unit is by the fluidized-bed gasification section (17) of bottom, jet Ji bed gasification section (18) and upper extension section (20) are formed, to jet fluidized bed gasification section by two dry-powder air-current bed reacting cylinder body of symmetry (18), fine breeze combustion mouth (15), vaporized chemical inlet pipe (14) and fine breeze concentrated phase transfer lime (13) constitute.
3. as the device of a kind of solid slag-discharing dry-powder air-current bed gasification process as described in the claim 2, it is characterized in that the element of cone of described grid distributor (4) and the angle β of central shaft are 20～50 degree, the hole on the grid distributor (4) be a circle.
4. as the device of a kind of solid slag-discharing dry-powder air-current bed gasification process as described in the claim 2-3, it is characterized in that the element of cone of described reducing pipe (5) and the angle γ of central shaft are the 5-20 degree.
5. as the device of a kind of solid slag-discharing dry-powder air-current bed gasification process as described in the claim 2-4, it is characterized in that described is 0～30 degree to spray powder air flow bed central shaft and the axle clamp angle α of vertical reactor main center, two central shaft point of contacts are apart from fluidized-bed sparger upper edge height L=0.5-2D, and D is a fluidized-bed concentrated phase section diameter.
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