CN102533345B - Method and device for coal gasification in combined type fluidized bed - Google Patents
Method and device for coal gasification in combined type fluidized bed Download PDFInfo
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- CN102533345B CN102533345B CN201110431593.3A CN201110431593A CN102533345B CN 102533345 B CN102533345 B CN 102533345B CN 201110431593 A CN201110431593 A CN 201110431593A CN 102533345 B CN102533345 B CN 102533345B
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Abstract
The invention discloses a method for coal gasification in a combined type fluidized bed, which comprises coal preparation, gas supply, gasification, slag discharge, dedusting, waste heat recovery and fine powder conveying. An ash agglomeration fluidized bed realizes gasification of large-particle coal; the non-completely converted carryover fine powder enters an entrained flow bed gasifier in a dense phase pneumatic conveying manner; secondary gasification is carried out by using a short retention time high temperature gasification manner; the produced ash slag is carried into an intersection segment of the fluidized bed and the entrained flow bed with high temperature coal gas, and rapidly mixed with ''low temperature'' large-particle partially carbonized coal in the fluidized bed and the produced ''low temperature'' coal gas; and partial ash slag is selectively discharged out of the gasifier in the form of solid. The method and the device of the invention have the advantage of being suitable for various coal types and high in carbon conversion rate.
Description
Affiliated field
The invention belongs to a kind of method and device of gasification, be specifically related to a kind of method and device that adopts fluidized-bed, the compound integrated effective fluidized bed coal-gasification of air flow bed.
Background technology
Gasification is one of core technology of coal high-efficiency, clean utilization, is the basis of the process industrials such as development coal-based chemicals, coal-based clean fuel, industrial combustion gas and polygenerations systeme.
Coal Gasification Technology development trend from Present Domestic, maximizing, pressurize, adapt to multiple fine coal, low pollution, easily purifying is gasification developing direction.The external existing pressurized gasification type of furnace is mainly divided three classes: pressurization static bed vapourizing furnace (as Lurgi stove), pressurized fluidized bed gasifier (HTW) and gasification furnace of pressurized aerated bed (Texaco, Shell, DOW, GSP).This three classes vapourizing furnace respectively has its relative merits, and it is raw material that pressurization static bed vapourizing furnace be take weak bonding lump coal, technology maturation, and in coal gas, methane content is high, cold gas efficiency is high, but purification system complicated (tar processing); Airflow bed gasification furnace high-temperature operation, gasification intensity and GAS QUALITY are high, but need take low ash, low-ash-fusion coal, are raw material, and oxygen consumption is high, facility investment is high; Fluidized-bed gasification furnace coal adaptability is wide, invests that low, oxygen consumption is low, scale is flexible, but coal gas entrained fines amount is high, total efficiency of carbon conversion low (90% left and right).
Shanxi Coal-Chemical Inst., Chinese Academy of Sciences has successfully developed " Unit of Coal Gasification for Pulverized Coal with Ash " complete set technology, coal wide ranges (from brown coal to hard coal), and be applicable to high ash, high ash melting point, high-sulfur coal gasification.Complete at present the industrial application of processing 100 tons of bituminous coal and 0.6MPa pressurization day 320 tons of Anthracites of processing normal pressure day, on pressurized gasification pilot plant, completed the molten gasification test that gathers of 0.6-2.5MPa hard coal pressurization ash simultaneously.Solved well ash discharge carbon content problem, but coal gas entrained fines amount is high, total efficiency of carbon conversion low (90% left and right).
Because the service temperature of fluidized-bed gasification furnace is 1000 ℃ of left and right, under this temperature condition, coal tar need have the 20-30 minute residence time to transform completely, but fine particle (< 0.1mm, accounting for 10% left and right into coal total amount) residence time in vapourizing furnace is conventionally within tens to tens second time, although increased fine powder circulation, total reaction times is short, and efficiency of carbon conversion is low.This part is unconverted, and fine powder is taken system out of, causes fluidized-bed carbon utilisation rate to decline.
Summary of the invention
First object of the present invention is to provide a kind of various coals that are suitable for, the efficient composite fluidized bed gasification method that efficiency of carbon conversion is high.
Second object of the present invention is to design a kind of by fluidized-bed and compound simple in structure, the composite fluidized bed gasification installation that cost is low of air flow bed.
The present invention is based on coal grading and transform thinking, with ash fusing fluidized bed gasification, realize macrobead coal gasification, the fine powder of taking out of not transforming completely passes through airflow bed gasification furnace, take short residence time(SRT), high-temperature gasification mode to carry out second gasification, and then total efficiency of carbon conversion and the processing power of raising system, reduce energy consumption and running cost, realizing high vaporization ability is target.It is few, the water-free semicoke fine powder of volatile content that unreacted is taken fine powder completely out of, and its granularity is close with dry coal powder airflow bed raw material, can enter air flow bed by the air conveying mode of concentrated phase.Fine powder gasifies under air flow bed section hot conditions, the lime-ash producing is carried and enters fluidized-bed and the air flow bed section of crossing with coal gas of high temperature, and mix with " low temperature " macrobead semicoke in fluidized-bed and " low temperature " coal gas producing rapidly, part lime-ash is discharged from vapourizing furnace selectively with solid-state form.
The method of coal gasification in combined type fluidized bed of the present invention comprises the steps:
(1) preparation of gasified raw material coal
Feed coal fragmentation, by super-dry and screening, makes moisture content of coal < 5wt%, and granularity is less than 6mm and sends into coal bunker as fluidized-bed gasification raw coal; Fine powder comes from gasification unreacted semicoke fine powder completely, the fine powder of secondary whirlwind, radiation waste heat boiler and High Temperature Ceramic Filter trapping;
(2) gasification
A. first vapourizing furnace is carried out to baker, treat that fluidized-bed gasification furnace temperature of lower is greater than 900 ℃, when upper temp is greater than 600 ℃, at fluidized-bed lower gas sparger, pass into air, steam, from vapourizing furnace underfeed mouth, add continuously gasification broken coal, and press air coal than 2.5～3.5Nm
3/ kg, steam coal operate than 0.3～0.6kg/kg, make coal in vapourizing furnace internal combustion, and obtain semicoke furnace charge, set up gradually material in vapourizing furnace stove, and now air flow bed is still in the baker stage, and remains on 850-900 ℃;
B. the bed pressure drop for the treatment of semicoke material in fluidized-bed gasification furnace reaches 5～10KPa, after system operation is stable, switches to oxygen/humidified blast, and in handoff procedure, temperature is controlled at 800～900 ℃;
C. press oxygen coal than 0.4～0.5Nm
3/ kg, steam coal operate than 0.5～1.0kg/kg, and fluidized-bed gasification furnace bottom temp is stabilized in 950～1050 ℃ of scopes;
D. after fluidized-bed gasification furnace bottom gasification is stable, fine powder is delivered to air flow bed burner noz(zle) by fine powder transfer pot, then passes into oxygen and steam to burner noz(zle), by oxygen dry pulverized coal than 0.5～0.7Nm
3/ kg, steam coal operate than 0.1～0.3kg/kg, and air flow bed service temperature is 1100～1300 ℃ of scopes, and the fluidized-bed in fluidized-bed and the air flow bed section of crossing temperature are 1050～1150 ℃ of scopes;
(3) deslagging of vapourizing furnace
In gasification, regulate annular separator tube gas speed at 5～10m/s, the oxygen concn < 25Vol% in gas; Central jet pipe gas speed 15～30m/s, the oxygen concn 40～60vol% in gas, makes the height that in vapourizing furnace, semicoke furnace charge keeps make bed pressure reduction between 4～8KPa;
(4) purification of raw gas and waste heat recovery
In vapourizing furnace outlet, spray into chilled water, guarantee 900 ℃ of whirlwind temperature in <, raw gas is separated through primary cyclone, the semicoke fine powder of trapping is through standpipe, high-temperature fine powder control valve, be blown into the concentrated phase fluidized-bed gasification section of pyrolytic gasification reactor lower part, again participate in reaction; Raw gas enters secondary cyclone, and the semicoke fine powder of trapping is sent in fine powder warehouse through semicoke fines collection/cooling tank, fine powder handling machinery; Coal gas of high temperature through roughing out enters radiation waste heat boiler, convection current exhaust-heat boiler and coal gas porcelain filter, gas temperature is down to 150-200 ℃ and is entered Venturi water scrubber and water-cooled eluting column, further after cooling and dedusting, export gas purification workshop section to, through the semicoke fine powder of radiation waste heat boiler and porcelain filter trapping, also through semicoke fines collection/cooling tank, fine powder handling machinery, send in fine powder warehouse;
(5) conveying of fine powder
Fine powder through secondary whirlwind, radiation waste heat boiler and porcelain filter trapping enters fine powder warehouse, through Pneumatic conveying pump, fine powder is delivered to the reinforced gravimetric tank of fine powder, and then enter the reinforced surge tank of fine powder and the reinforced transfer pot of fine powder, by nitrogen, blow and fine powder is sent into air flow bed burner noz(zle) gasify.
5. vapourizing furnace stops
During orderly shutdown, the oxygen of closed gas flow bed burner noz(zle), then stop fine powder conveying, and open the quantity of steam of large-scale combustion nozzle simultaneously, play the effect that protection nozzle, purging and air flow bed are partly lowered the temperature; Cut-out enters the gas line of rear system, and coal gas emptying is depressurized to normal pressure gradually; Afterwards, reduce fluidized-bed ring pipe gas speed and strengthen ash discharge amount, strengthen fluidized bed steam consumption simultaneously, close oxygen valve, close the coal measures that enters of fluidized-bed and unite, in stove, temperature is controlled at below 900 ℃; After furnace charge is drained, stop air inlet, final system is used respectively steam, air purge one time.
For realize the present invention designed a kind of simple in structure, the coal gasification in combined type fluidized bed device that cost is low.
Composite fluidized bed gasification installation of the present invention is by coal gasification in combined type fluidized bed stove, semicoke fine powder circulation device forms, described coal gasification in combined type fluidized bed stove is comprised of fluidized-bed and air flow bed, fluidized-bed is by fluidized-bed body of heater, gasifier gas outlet pipe, gas distributor and annular release ash tube form, there are gasifier gas outlet pipe and furnace roof Quench water pipe in fluidized-bed body of heater top, coal feed-pipe is arranged at fluidized-bed body of heater bottom, fluidized-bed body of heater bottom connects gas distributor, under gas distributor, be connected with annular release ash tube, the bottom of fluidized-bed body of heater is ash fusing fluidized bed gasification section, middle part is fluidized-bed and the air flow bed section of crossing, top is expanding reach, air flow bed is by air flow bed body of heater, air flow bed burner noz(zle) and steam connection tube form, air flow bed burner noz(zle) is positioned at air flow bed body of heater top, steam connection tube is positioned at air flow bed body of heater middle part, air flow bed lower portion of furnace body is connected by coal gas of high temperature pipe connecting with the air flow bed section of crossing with the fluidized-bed at fluidized-bed middle part, semicoke fine powder circulation device is by primary cyclone, semicoke fine powder cycle control high-temperature valve forms, primary cyclone top is connected with gasifier gas outlet pipe, primary cyclone bottom is connected with semicoke fine powder circulating solid tube, semicoke fine powder cycle control high-temperature valve upper end is connected with semicoke fine powder circulating solid tube, lower end is connected with semicoke fine powder feed-pipe, on semicoke fine powder feed-pipe, there is fine powder to return to steam gas blow pipe, semicoke fine powder feed-pipe is connected with fluidized-bed body of heater bottom.
Air flow bed body of heater as above and fluidized-bed body of heater are by steel furnace shell, and refractory materials and lagging material form, and lagging material is between steel furnace shell and refractory materials.
Gas distributor as above has pipe core vaporized chemical inlet pipe and grid distributor vaporized chemical inlet pipe,
The bottom of annular release ash tube as above is slag-drip opening, and there is annular release pipe vaporized chemical inlet pipe at the middle part of annular release ash tube.
Air flow bed burner noz(zle) as above is connected with fine powder concentrated phase transfer lime and entrained flow gasification agent inlet pipe.
Tool of the present invention has the following advantages:
1) vapourizing furnace working pressure can reach 3.0MPa, and treatment capacity is large, and compression energy consumption is low;
2) adopt selectivity ash content from, dry cinder discharging, ash discharge carbon content is low;
3) fine powder that coal gas is entrained with is after circulation, and at high temperature gasification again, reaches completely and transform, and then improves total efficiency of carbon conversion of gasification;
4) airflow bed gasification furnace operates at nearly ash fusion point temperature, and the high-temperature fine ash of generation enters rapidly the fluidized-bed section of crossing, and realizes with the cold slag of Jiao, and dry cinder discharging process makes full use of sensible heat simultaneously, and coal gas of high temperature and hot grey sensible heat are used for to coal gasification reaction;
5) can improve fluidized-bed gasification efficiency and processing power, can improve effective composition of coal gas simultaneously;
6) structure of reactor is simple, and without special refractory, cost is low; Simple to operate, long service life;
7) coal wide ranges, the most of coals of gasifiable China.
accompanying drawing explanation
Fig. 1 is coal gasification in combined type fluidized bed apparatus structure schematic diagram
Fig. 2 is coal gasification in combined type fluidized bed process flow sheet
As shown in the figure, 1 is gas distributor, centered by 2, manage vaporized chemical inlet pipe, 3 is annular release pipe vaporized chemical inlet pipe, 4 is slag-drip opening, 5 is annular release ash tube, 6 is grid distributor vaporized chemical inlet pipe, 7 is steel furnace shell, 8 is refractory materials, 9 is lagging material, 10 is coal feed-pipe, 11 is ash fusing fluidized bed gasification section, 12 is fluidized-bed and the air flow bed section of crossing, 13 is expanding reach, 14 is furnace roof Quench water pipe, 15 is gasifier gas outlet pipe, 16 is primary cyclone, 17 is semicoke fine powder circulating solid tube, 18 is semicoke fine powder cycle control high-temperature valve, 19 return to steam gas blow pipe for fine powder, 20 is semicoke fine powder feed-pipe, 21 is fine powder concentrated phase transfer lime, 22 is entrained flow gasification agent inlet pipe, 23 is air flow bed burner noz(zle), 24 is entrained flow gasification section, 25 is steam connection tube, 26 is coal gas of high temperature pipe connecting, 27 is upper coal rotary conveyor, 28 is vibrating screen classifier, 29 is crusher, 30 is moisture eliminator, 31 is moisture-free coal 1# rotary conveyor, 32 is moisture-free coal 1# lift, 33 is moisture-free coal warehouse, 34 is moisture-free coal 2# rotary conveyor, 35 is moisture-free coal 2# lift, 36 is moisture-free coal balance bucket, 37 is moisture-free coal coal feeding bucket, 38 is rotary feeder, 39 is fluidized-bed gasification furnace, 40 is airflow bed gasification furnace, 41 is slag bucket on deslagging, 42 is slag bucket under deslagging, 43 is secondary cyclone, 44 is secondary cyclone trapping fine powder surge tank, 45 is two to revolve thin collection and transfer pot, 46 is heating gas radiation waste heat recovery boiler, 47 is heating gas convection current heat recovery boiler, 48 is waste heat boiler bubble, 49 is radiant boiler trapping fine powder surge tank, 50 is radiant boiler trapping fines collection and transfer pot, 51 is coal gas porcelain filter, 52 is porcelain filter trapping fine powder surge tank, 53 is porcelain filter trapping fines collection and transfer pot, 54 is Venturi scrubber, 55 is column plate type washing tower, 56 is flashing tower, 57 is air water separator, 58 is thick thionizer, 59 is coal gas pressure regulator valve, 60 for carrying fine powder sack cleaner, 61 for carrying fine powder buffering/weighing apparatus, 62 is fine powder warehouse, 63 is fine powder Pneumatic conveying pump, 64 is reinforced fine powder sack cleaner, 65 is the reinforced gravimetric tank of fine powder, 66 is the reinforced surge tank of fine powder, 67 is the reinforced transfer pot of fine powder, 68 is superheated vapour steam distributor, 69 is oxygen sub-cylinder, 70 is air sub-cylinder.
Embodiment
Gasification process of the present invention and specific equipment accompanying drawings thereof are as follows:
Embodiment 1:
Composite fluidized bed gasification installation is by coal gasification in combined type fluidized bed stove, semicoke fine powder circulation device forms, described coal gasification in combined type fluidized bed stove is comprised of fluidized-bed and air flow bed, fluidized-bed is by fluidized-bed body of heater, gasifier gas outlet pipe 15, gas distributor 1 and annular release ash tube 5 form, fluidized-bed body of heater is by steel furnace shell 7, refractory materials 8 and lagging material 9 are made, lagging material 9 is between steel furnace shell 7 and refractory materials 8, there are gasifier gas outlet 15 and furnace roof Quench water pipe 14 in fluidized-bed body of heater top, coal feed-pipe 10 is arranged at fluidized-bed body of heater bottom, fluidized-bed body of heater bottom connects gas distributor 1, gas distributor 1 has pipe core vaporized chemical inlet pipe 2 and grid distributor vaporized chemical inlet pipe 6, under gas distributor 1, be connected with annular release ash tube 5, the bottom of annular release ash tube 5 is slag-drip opening 4, there is annular release pipe vaporized chemical inlet pipe 3 at the middle part of annular release ash tube 5.The bottom of fluidized-bed body of heater is that ash fusing fluidized bed gasification section 11, middle part are that fluidized-bed and the air flow bed section of crossing 12, top are expanding reach 13, air flow bed is by air flow bed body of heater, air flow bed burner noz(zle) 23 and steam connection tube 25 form, and air flow bed burner noz(zle) 23 is connected with fine powder concentrated phase transfer lime 21 and entrained flow gasification agent inlet pipe 22.Air flow bed burner noz(zle) 23 is positioned at air flow bed body of heater top, steam connection tube 25 is positioned at air flow bed body of heater middle part, air flow bed lower portion of furnace body is connected by coal gas of high temperature pipe connecting 26 with the air flow bed section of crossing 12 with the fluidized-bed at fluidized-bed middle part, semicoke fine powder circulation device is by primary cyclone 16, semicoke fine powder cycle control high-temperature valve 18 forms, primary cyclone 16 tops are connected with gasifier gas outlet pipe 15, primary cyclone 16 bottoms and semicoke fine powder circulating solid tube 17, semicoke fine powder cycle control high-temperature valve 18 upper ends are connected with semicoke fine powder circulating solid tube 17, lower end is connected with semicoke fine powder feed-pipe 20, on semicoke fine powder feed-pipe 20, there is fine powder to return to steam gas blow pipe 19, semicoke fine powder feed-pipe 20 is connected with fluidized-bed body of heater bottom.
Raw coal is sent into vibrating screen classifier 28 through upper coal rotary conveyor 27, the raw coal that granularity is greater than 6mm is crushed to through crusher 29 coal that granularity is less than 6mm, enter moisture eliminator 30 dry together with raw coal under the sieve of vibrating screen classifier 28, the moisture content < 5wt% in coal.Dry by moisture-free coal 1# rotary conveyor 31, moisture-free coal 1# lift 32, enters moisture-free coal warehouse 33 stand-by.
First vapourizing furnace is carried out to baker, baker air is from air sub-cylinder 70, the baker fuel of fluidized-bed is diesel oil, the baker fuel of air flow bed is methyl alcohol, air is respectively by grid distributor vaporized chemical inlet pipe 6, pipe core vaporized chemical inlet pipe 2, annular release pipe vaporized chemical inlet pipe 3 enters fluidized-bed gasification furnace; Air enters fine powder burner noz(zle) 23 by entrained flow gasification agent inlet pipe 22 and burns in air flow bed with methanol mixed.Treat that fluidized-bed gasification furnace bottom dense phase fluidized bed gasification section 11 temperature reach 910 ℃, top expanding reach temperature reaches after 620 ℃, by each road inlet pipe 2,3,6, passes into air 2500Nm
3/ h and steam 400kg/h (steam comes from superheated vapour steam distributor 68), open rotary feeder 38 and quantitatively add continuously gasification of coal from gasification furnace coal feed-pipe 10, keeps coal input quantity 1000kg/h, air capacity 2500Nm
3/ h, quantity of steam 400kg/h.Set up bed (bed in about pressure reduction 6KPa), when temperature, pressure, flow system all reach after imposing a condition, switch to oxygen/humidified blast, oxygen comes from oxygen sub-cylinder 69, oxygen feeding amount 500Nm
3/ h, water vapor amount 1000kg/h, in handoff procedure, temperature is controlled at, and 870 ℃, then slowly regulate oxygen, steam flow, progressively regulate gasification system pressure to 0.6MP, regulate coal input quantity to 1500kg/h simultaneously, amount of oxygen is to 750Nm
3/ h, quantity of steam is to 1500kg/h, and temperature-stable is at 950 ℃.Now air flow bed is still in the baker stage, and remains on 920 ℃.
After system stability, fine powder is delivered to air flow bed burner noz(zle) 23 by the reinforced transfer pot 67 of fine powder, then passes into oxygen and steam to burner noz(zle) 23, fine powder intake is 200kg/h, by oxygen dry pulverized coal, compares 0.55Nm
3/ kg, steam coal operate than 0.15kg/kg, and air flow bed part operation temperature is at 1180 ℃.Fluidized-bed and the air flow bed section of crossing temperature are at 1120 ℃.
Lime-ash in vapourizing furnace 39 enters on deslagging slag bucket 42 under slag bucket 41 and deslagging through vapourizing furnace bottom ash tube 5, and regularly from deslagging, slag bucket 42 is discharged lime-ash.In operational process, by adjusting the chilled water flow in furnace roof Quench water pipe 14, guarantee that coal gas is 900 ℃ of vapourizing furnace temperature out <.Raw gas is through primary cyclone 16 separation, the semicoke fine powder of trapping is through semicoke fine powder circulating solid tube 17, semicoke fine powder cycle control high-temperature valve 18, by fine powder, returned to the steam that steam gas blow pipe 19 passes into and be blown into vapourizing furnace dense phase fluidized bed gasification section 11, again participate in reaction; Raw gas enters secondary cyclone 43, and the semicoke fine powder of trapping revolves thin collection and transfer pot 45 is sent into fine powder warehouse 62 through secondary cyclone trapping fine powder surge tank 44, two; Coal gas of high temperature after roughing out enters heating gas radiation waste heat recovery boiler 46, convection current heat recovery boiler 47 and coal gas porcelain filter 51, at the interior part fine powder of radiant boiler 46, be captured, enter radiant boiler trapping fine powder surge tank 49 and radiant boiler trapping fines collection and transfer pot 50 and send into fine powder warehouse 62, the fine powder trapping in porcelain filter is through porcelain filter trapping fine powder surge tank 52 and porcelain filter traps fines collection and transfer pot 53 is sent into fine powder warehouse 62; Gas temperature is down to 150-200 ℃ and is entered Venturi water scrubber 54, column plate type washing tower 55, air water separator 57, thick thionizer 58, and further cooling and desulfurization export gas purification workshop section to by coal gas pressure regulator valve 59.
During orderly shutdown, the oxygen of closed gas flow bed burner noz(zle) 23, then stop fine powder conveying, and open the quantity of steam of large-scale combustion nozzle 23 simultaneously, play the effect that protection nozzle, purging and air flow bed are partly lowered the temperature; Cut-out enters the gas line of rear system, and coal gas emptying is depressurized to normal pressure gradually; Afterwards, reduce fluidized-bed ring pipe gas speed and strengthen ash discharge amount, strengthen fluidized bed steam consumption simultaneously, close oxygen valve, close the coal measures that enters of fluidized-bed and unite, in stove, temperature is controlled at below 900 ℃; After furnace charge is drained, stop air inlet, final system is used respectively steam, air purge one time.
Embodiment 2:
Fluidized-bed coal input quantity 2300kg/h, oxygen feeding amount 1100Nm
3/ h, water vapor amount 2000kg/h, air flow bed fine powder inlet amount 400kg/h, compares 0.53Nm by oxygen dry pulverized coal
3/ kg, steam coal operate than 0.16kg/kg, and vapourizing furnace pressure-controlling is at 1.0MPa, and fluidized-bed gasification furnace bottom temp is stabilized in 980 ℃, and air flow bed part operation temperature is at 1250 ℃, and fluidized-bed and the air flow bed section of crossing temperature are at 1100 ℃.All the other are with embodiment 1.
Embodiment 3:
Fluidized-bed coal input quantity 2800kg/h, oxygen feeding amount 1380Nm
3/ h, water vapor amount 2700kg/h, air flow bed fine powder inlet amount 600kg/h, compares 0.55Nm by oxygen dry pulverized coal
3/ kg, steam coal operate than 0.16kg/kg, and vapourizing furnace pressure-controlling is at 1.5MPa, and fluidized-bed gasification furnace bottom temp is stabilized in 1000 ℃, and air flow bed part operation temperature is at 1200 ℃, and fluidized-bed and the air flow bed section of crossing temperature are at 1090 ℃.All the other are with embodiment 1.
Embodiment 4:
Fluidized-bed coal input quantity 3300kg/h, oxygen feeding amount 1600Nm
3/ h, water vapor amount 3150kg/h, vapourizing furnace middle part fine breeze inlet amount 700kg/h, compares 0.54Nm by oxygen dry pulverized coal
3/ kg, steam coal operate than 0.158kg/kg, and vapourizing furnace pressure-controlling is at 2.0MPa, and fluidized-bed gasification furnace bottom temp is stabilized in 1030 ℃, and air flow bed part operation temperature is at 1100 ℃, and fluidized-bed and the air flow bed section of crossing temperature are at 1050 ℃.All the other are with embodiment 1.
Embodiment 5:
Fluidized-bed coal input quantity 3700kg/h, oxygen feeding amount 1800Nm
3/ h, water vapor amount 3560kg/h, vapourizing furnace middle part fine breeze inlet amount 800kg/h, compares 0.7Nm by oxygen dry pulverized coal
3/ kg, steam coal operate than 0.3kg/kg, and vapourizing furnace pressure-controlling is at 2.5MPa, and fluidized-bed gasification furnace bottom temp is stabilized in 1000 ℃, and air flow bed part operation temperature is at 1300 ℃, and fluidized-bed and the air flow bed section of crossing temperature are at 1150 ℃.All the other are with embodiment 1.
As table 1 is listed in the New Solid deslagging dry-powder air-current bed coal-gasification preparing synthetic gas gas composition of carrying out under embodiment 1-5 condition.
Gasifying multi-segment staged converted fluidized bed preparing synthetic gas gas composition under table 1 different condition
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Embodiment 2 | |
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| Vapor pressure, MPa | 0.6 | 1.0 | 1.5 | 2.0 | 2.5 |
| Fluidized-bed coal input quantity, kg/h | 1500 | 2300 | 2800 | 3300 | 3700 |
| Air flow bed fine powder amount, kg/h | 300 | 400 | 600 | 700 | 800 |
| Total oxygen feeding amount, Nm 3/h | 860 | 1312 | 1710 | 1978 | 2360 |
| Total quantity of steam, kg/h | 1530 | 2064 | 1796 | 3260.6 | 3800 |
| Dry gas forms Vol.% | |||||
| H 2 | 36.43 | 38.04 | 37.72 | 37.23 | 37.98 |
| N 2 | 8.8 | 5.17 | 5.54 | 6.05 | 5.57 |
| CO | 24.36 | 25.62 | 26.85 | 26.8 | 28.16 |
| CH 4 | 4.61 | 5.17 | 5.09 | 5.32 | 5.69 |
| CO 2 | 25.8 | 26 | 24.8 | 24.6 | 22.6 |
| Factor of created gase Nm3/kg | 2.04 | 2.03 | 2.04 | 2.05 | 2.07 |
| Caloric power of gas Kcal/Nm 3 | 2073.4 | 2192.7 | 2243.77 | 2320.8 | 2352.8 |
| Efficiency of carbon conversion % | 93.5 | 93 | 93.2 | 93.6 | 94 |
| Cold gas efficiency % | 73.67 | 73.42 | 73.51 | 74.21 | 74.39 |
Claims (6)
1. a method for coal gasification in combined type fluidized bed, is characterized in that comprising the steps:
(1) preparation of gasified raw material coal
Feed coal fragmentation, by super-dry and screening, makes moisture content of coal <5wt%, and granularity is less than 6mm and sends into coal bunker as fluidized-bed gasification raw coal; Fine powder comes from gasification unreacted semicoke fine powder completely, the fine powder of secondary whirlwind, radiation waste heat boiler and the trapping of coal gas porcelain filter;
(2) gasification
A. first vapourizing furnace is carried out to baker, treat that fluidized-bed gasification furnace temperature of lower is greater than 900 ℃, when upper temp is greater than 600 ℃, at fluidized-bed lower gas sparger, pass into air, steam, from vapourizing furnace underfeed mouth, add continuously gasification broken coal, and press air coal than 2.5～3.5Nm
3/ kg, steam coal operate than 0.3～0.6kg/kg, make coal in vapourizing furnace internal combustion, and obtain semicoke furnace charge, set up gradually material in vapourizing furnace stove, and now air flow bed is still in the baker stage, and remains on 850～900 ℃;
B. the bed pressure drop for the treatment of semicoke material in fluidized-bed gasification furnace reaches 5～10KPa, after system operation is stable, switches to oxygen/humidified blast, and in handoff procedure, temperature is controlled at 800～900 ℃;
C. press oxygen coal than 0.4～0.5Nm
3/ kg, steam coal operate than 0.5～1.0kg/kg, and fluidized-bed gasification furnace bottom temp is stabilized in 950～1050 ℃ of scopes;
D. after fluidized-bed gasification furnace bottom gasification is stable, fine powder is delivered to air flow bed burner noz(zle) by the reinforced transfer pot of fine powder, then passes into oxygen and steam to burner noz(zle), by oxygen dry pulverized coal than 0.5～0.7Nm
3/ kg, steam coal operate than 0.1～0.3kg/kg, and air flow bed service temperature is 1100～1300 ℃ of scopes, and the fluidized-bed in fluidized-bed and the air flow bed section of crossing temperature are 1050～1150 ℃ of scopes;
(3) deslagging of vapourizing furnace
In gasification, regulate annular separator tube gas speed at 5～10m/s, the oxygen concn <25Vol% in gas; Central jet pipe gas speed 15～30m/s, the oxygen concn 40～60vol% in gas, makes the height that in vapourizing furnace, semicoke furnace charge keeps make bed pressure reduction between 4～8KPa;
(4) purification of raw gas and waste heat recovery
At vapourizing furnace furnace roof, spray into chilled water, guarantee <900 ° of C of whirlwind temperature in, raw gas is separated through primary cyclone, the semicoke fine powder of trapping is through standpipe, high-temperature fine powder control valve, be blown into the concentrated phase fluidized-bed gasification section of pyrolytic gasification reactor lower part, again participate in reaction; Raw gas enters secondary cyclone, and the semicoke fine powder of trapping is sent in fine powder warehouse through semicoke fines collection/cooling tank, fine powder handling machinery; Coal gas of high temperature through roughing out enters radiation waste heat boiler, convection current exhaust-heat boiler and coal gas porcelain filter, gas temperature is down to 150～200 ℃ and is entered Venturi water scrubber and water-cooled eluting column, further after cooling and dedusting, export gas purification workshop section to, through the semicoke fine powder of radiation waste heat boiler and the trapping of coal gas porcelain filter, also through semicoke fines collection/cooling tank, fine powder handling machinery, send in fine powder warehouse;
(5) conveying of fine powder
Fine powder through secondary whirlwind, radiation waste heat boiler and the trapping of coal gas porcelain filter enters fine powder warehouse, through Pneumatic conveying pump, fine powder is delivered to the reinforced gravimetric tank of fine powder, and then enter the reinforced surge tank of fine powder and the reinforced transfer pot of fine powder, by nitrogen, blow and fine powder is sent into air flow bed burner noz(zle) gasify;
(6) vapourizing furnace stops
During orderly shutdown, the oxygen of closed gas flow bed burner noz(zle), then stop fine powder conveying, and open the quantity of steam of large-scale combustion nozzle simultaneously, play the effect that protection nozzle, purging and air flow bed are partly lowered the temperature; Cut-out enters the gas line of rear system, and coal gas emptying is depressurized to normal pressure gradually; Afterwards, reduce fluidized-bed ring pipe gas speed and strengthen ash discharge amount, strengthen fluidized bed steam consumption simultaneously, close oxygen valve, close the coal measures that enters of fluidized-bed and unite, in stove, temperature is controlled at below 900 ℃; After furnace charge is drained, stop air inlet, final system is used respectively steam, air purge one time.
2. as the composite fluidized bed gasification installation of the method for a kind of coal gasification in combined type fluidized bed claimed in claim 1, it is by coal gasification in combined type fluidized bed stove, semicoke fine powder circulation device forms, it is characterized in that described coal gasification in combined type fluidized bed stove is comprised of fluidized-bed and air flow bed, fluidized-bed is by fluidized-bed body of heater, gasifier gas outlet pipe (15), gas distributor (1) and annular release ash tube (5) form, there are gasifier gas outlet (15) and furnace roof Quench water pipe (14) in fluidized-bed body of heater top, coal feed-pipe (10) is arranged at fluidized-bed body of heater bottom, fluidized-bed body of heater bottom connects gas distributor (1), under gas distributor (1), be connected with annular release ash tube (5), the bottom of fluidized-bed body of heater is ash fusing fluidized bed gasification section (11), middle part is fluidized-bed and the air flow bed section of crossing (12), top is expanding reach (13), air flow bed is by air flow bed body of heater, air flow bed burner noz(zle) (23) and steam connection tube (25) form, air flow bed burner noz(zle) (23) is positioned at air flow bed body of heater top, steam connection tube (25) is positioned at air flow bed body of heater middle part, air flow bed lower portion of furnace body is connected by coal gas of high temperature pipe connecting (26) with the air flow bed section of crossing (12) with the fluidized-bed at fluidized-bed middle part, semicoke fine powder circulation device is by primary cyclone (16), semicoke fine powder cycle control high-temperature valve (18) forms, primary cyclone (16) top is connected with gasifier gas outlet pipe (15), primary cyclone (16) bottom is connected with semicoke fine powder circulating solid tube (17), semicoke fine powder cycle control high-temperature valve (18) upper end is connected with semicoke fine powder circulating solid tube (17), lower end is connected with semicoke fine powder feed-pipe (20), on semicoke fine powder feed-pipe (20), there is fine powder to return to steam gas blow pipe (19), semicoke fine powder feed-pipe (20) is connected with fluidized-bed body of heater bottom.
3. the composite fluidized bed gasification installation of the method for a kind of coal gasification in combined type fluidized bed as claimed in claim 2, it is characterized in that described fluidized-bed body of heater is by steel furnace shell (7), refractory materials (8) and lagging material (9) are made, and lagging material (9) is positioned between steel furnace shell (7) and refractory materials (8).
4. the composite fluidized bed gasification installation of the method for a kind of coal gasification in combined type fluidized bed as claimed in claim 2, is characterized in that described gas distributor (1) has pipe core vaporized chemical inlet pipe (2) and grid distributor vaporized chemical inlet pipe (6).
5. the composite fluidized bed gasification installation of the method for a kind of coal gasification in combined type fluidized bed as claimed in claim 2, the bottom that it is characterized in that described annular release ash tube (5) is slag-drip opening (4), and there is annular release pipe vaporized chemical inlet pipe (3) at the middle part of annular release ash tube 5.
6. the composite fluidized bed gasification installation of the method for a kind of coal gasification in combined type fluidized bed as claimed in claim 2, is characterized in that described air flow bed burner noz(zle) (23) is connected with fine powder concentrated phase transfer lime (21) and entrained flow gasification agent inlet pipe (22).
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