CN101372635B - High-density pressurized fluidized bed coal gasification apparatus and method - Google Patents
High-density pressurized fluidized bed coal gasification apparatus and method Download PDFInfo
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- CN101372635B CN101372635B CN2008101551063A CN200810155106A CN101372635B CN 101372635 B CN101372635 B CN 101372635B CN 2008101551063 A CN2008101551063 A CN 2008101551063A CN 200810155106 A CN200810155106 A CN 200810155106A CN 101372635 B CN101372635 B CN 101372635B
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Abstract
A high-density pressurized fluid bed coal gasification device and a method relate to a gasification device and a method which are especially suitable for the efficient treatment of the high-sulfur, high-ash and high ash fusion point coal with high reserve volume in China and have the advantages of broad coal type adaptability, high carbon transformation ratio in the gasification process, high heat value of coal gas, low investment and excellent environment-friendly performance. A gasification reactor (1) is arranged in a pressure shell (2) and is divided into a dense-phase turbulent flow fluidizing section (9), a high-density core-annulus flow section (10) and a density rapid flow section (11) from bottom to top, and according to the gasification character of the goal with high sulfur, high ash and high ash fusion point, flow states with different features are adopted for pressurizing and sectionalized gasification from bottom to top and the pressure for gasification is 1.0-2.5MPa.
Description
Technical field
The present invention relates to a kind of high-density pressurized fluidized bed coal gasification apparatus and method, belong to the Coal Gasification Technology field.
Technical background
Gasification can solve the pollution problem in the direct combustion processes of coal better, is the cleanest coal fired power generation mode as integrated gasification combined cycle plants; Moreover, gasification can also form the product of high value, as being the Chemical Manufacture of raw material with the coal, especially to produce synthetic ammonia, methyl alcohol, system H
2With liquid fuel etc., in China's energy strategy, play important status.
At present, industrialized coal gasification apparatus mainly contains fixed bed, fluidized-bed and airflow bed gasification furnace three major types type.These gasifying process all have it that the shortcoming and the scope of application are arranged: (1) airflow bed gasification furnace is a current development gasifying process faster, its feature is the efficiency of carbon conversion height, cold gas efficiency and thermo-efficiency are than other gasifying process height, and be suitable for maximizing and produce, the day of maximum separate unit vapourizing furnace handle the coal amount and can reach 2000～3000 tons; But because it is a slag tap, therefore only be applicable to the coal of ash fusion point less than 1400 degree, also inapplicable to the coal of high ash, high ash melting point; The oxygen that gasifies in addition consumption is also than other technology height; (2) advantage of fixed-bed gasification furnace is that unit consumption of energy is smaller, and coal is had the subject range of broad, and thermo-efficiency is higher; But fixed bed gasification technology has strict requirement to the granularity of coal, be only applicable to the gasification of weak cohesiveness lump coal or moulded coal, and for preventing slagging scorification, service temperature is lower, and the water vapor consumption is big, and the by product tar of generation and phenol are difficult to handle; In addition, because its gasification intensity is lower, maximizing is subjected to certain restriction; (3) characteristics of fluidized-bed gasification furnace are relatively wide to coal adaptability, comprise the coal of high ash, low heat value and high ash melting point, and gasification oxygen consumption is lower, is suitable for air gasification and oxygen-rich gasification; The problem that exists is at present: and amplification performance industrialized KRW and the U-Gas type of furnace better to coal adaptability is subjected to certain restriction; Supercharging bubbling fluidized bed (as HTW) and circle fluidized-bed gasification furnace successfully have been amplified to 740 tons of day processing coal amounts, when the two is only applicable to viscosity coal preferably.
The coal resources of China not only distribute extensively, type is many, and three high coal (high ash melting point, high ash, high-sulfur) accounts for very big ratio in the total reserves of coal, wherein high-ash-fusion coal accounts for 50% of total reserves, sulphur content accounts for 20～40% above 2% high sulphur coal, and the average ash content in the coal is greater than 20%.Existing gasifying process can't directly apply to the abundant high-sulfur of China's reserves, high ash, high ash melting point coal gasification, therefore need exploitation badly coal adaptability extensively is particularly 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 advanced gasification technology.
Summary of the invention
Technical problem: the problem that on high-sulfur, high ash, high ash melting point gasification, exists at present various gasification technologies, the present invention proposes a kind of high-density pressurized fluidized bed coal gasification 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: high-density pressurized fluidized bed coal gasification apparatus of the present invention mainly is made up of gasifying reactor, two-stage efficient cyclone separator, two-stage returning charge valve etc.Gasifying reactor is built by laying bricks or stones by refractory brick or refractory material casting forms, and is arranged in the pressure vessel, is filled with thermal insulation layer between pressure vessel and the reactor; Reactor is divided into close phase turbulent flow fluidisation section, high-density nucleolus flow sections, the quick flow sections of high-density from bottom to top.The top of close phase turbulent flow fluidisation section is provided with one-level returning charge mouth, and the bottom is provided with coal and Wingdale import, and the bottom is provided with air distribution plate and scum pipe; Even for close phase turbulent flow fluidisation Duan Bufeng, deslagging is smooth and easy and prevent high-temperature coking, wind cap and peripheral fluidisation blast cap in the middle of being equipped with on the air distribution plate, the air distribution plate bottom is an air compartment, air compartment is made up of middle air compartment and peripheral air compartment; Middle air compartment bottom is provided with thin ash discharging hole and superheated vapour inlet; The periphery air compartment is provided with main vaporized chemical import, and the bottom is provided with two thick ash discharging holes; Air compartment and pressure vessel led to outside the stove in the middle of scum pipe passed.High-density nucleolus flow sections is the amplification thorax body between close phase turbulent flow fluidisation section and the quick flow sections of high-density, and the bottom is provided with one-level second gasification agent import, and the middle part is provided with secondary second gasification agent import, and secondary returning charge mouth is arranged on one-level second gasification agent import top.The diameter of the quick flow sections of high-density is identical with close phase turbulent flow fluidisation section section, the reactor outlet of its upper side links to each other with the one-level efficient cyclone separator, the bottom of separator is connected to the one-level material blanking tube, the bottom of material blanking tube is connected to one-level returning charge valve, and its revert pipe becomes 30～45 degree to be connected one-level returning charge mouth with reactor axis; The outlet on one-level efficient cyclone separator top is connected to the secondary efficient cyclone separator, become 60～90 degree with the one-level efficient cyclone separator and in higher location arrangements, the bottom of separator is connected to the secondary material blanking tube, the bottom of material blanking tube is connected to secondary returning charge valve, and its revert pipe becomes 30～45 degree to be connected secondary returning charge mouth with reactor axis.
High-density pressurized fluidized bed coal gasification method of the present invention is different fully with the technical scheme of existing technology, concrete mode is: according to the vaporization characteristic of high-sulfur, high ash, high-ash-fusion coal, the segmented gasification that pressurizes under the fluidised form of different characteristics, vapor pressure is 1.0～2.5MPa.Close phase turbulent flow fluidisation section is that solids volume concentration 0.3～0.45, bed depth are the emulsion zone of 2～5m, adopt the turbulent flow fluidisation operation scheme of temperature 850～1050 degree, gas speed 1～1.5m/s, its function is to realize the well blend and the caloic transmission of bed material, coal and Wingdale, vaporized chemical and one-level returning charge, and devolatilization, burning and the partial gasification reaction of carrying out coal; It is 0～3mm inert bed material that the bed material adopts particle diameter; Coal adds from the close fluidisation of turbulent flow mutually section with Wingdale, and adopting particle diameter is the particle of 0～10mm; Vaporized chemical forms for the air of the superheated vapour of gasification required 80～93% and 100% or pure oxygen or oxygen-rich air mix, the mode that vaporized chemical adopts classification to add, 30～50% vaporized chemical adds from the I and II second gasification agent import of high-density nucleolus flow sections, and 50～70% vaporized chemical adds from the main vaporized chemical import of peripheral air compartment.The quick flow sections of high-density nucleolus flow sections and high-density is the main section of gasification reaction and desulphurization reaction, and the semicoke that generates behind the close phase turbulent flow fluidisation section partial gasification is at this section gasification, the H that Wingdale produces gasification
2S removes.The mobile operation scheme of high-density nucleolus that high-density nucleolus flow sections height is 5～8m, employing temperature 1000～1200 is spent, solids volume concentration is 0.1～0.2 gentle fast 1.5～2m/s; This section cross section is bigger, by in this section, the bottom adds the second gasification agent and the bottom adds the secondary returning charge, form the high-density nucleolus and flow, the slippage of near wall district gas-solid and back-mixing have been strengthened the interaction between the gas-solid, can improve gasification reaction and sulfurous pollutants removes speed.The quick flow sections height of high-density is 3～5m, adopts about temperature 1100 degree, solids volume concentration is greater than the high-density of the 0.1 gentle fast 2.5～3m/s operation scheme that flows fast; The fast mobile formed turbulence of sufficiently high reaction section and high-density has guaranteed the particulate profit reduction and reserving time, and efficiency of carbon conversion and pollutant removing efficient are improved.The solid particulate that adopts the two-stage efficient cyclone separator to separate to generate in the coal gas (being mainly CaS that coke, the desulfurization completely of flying dust, unreacted produce and thin inert bed material etc.), making particle diameter be that particle more than 10 microns is all separated gets off, total efficiency of separation is greater than 99%, wherein the first step is greater than 95%, and the second stage is greater than 85%.Take independent returning charge mode, first step returning charge enters close phase turbulent flow fluidisation section, and second stage returning charge enters high-density nucleolus flow sections, and the two-stage returning charge is not disturbed mutually; Returning charge elegance 2～5% required superheated vapours of gasification; In addition, for improving the flowability of returning charge, in revert pipe, add the thin bed material of 200 microns following inertia of a certain amount of particle diameter, carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation with guarantee that the two-stage returning charge amounts to the high circulation ratio more than 50, make not react completely semicoke and Wingdale.The slag particle that gasification produces is discharged by scum pipe, air compartment in the middle of 5～15% superheated vapours that gasify required feed, enter gasifying reactor via middle wind cap, the slag particle that gasification produces blows in the orientation of superheated vapour and enters scum pipe down smoothly, be interrupted or discharge continuously by residue extraction mechanism, this superheated vapour also can play thermoregulatory effect, and the temperature by the amount that adds superheated vapour is regulated the air distribution plate zone prevents high-temperature coking; Because the thin ash of air compartment or slag or inert bed material were discharged by the thin ash discharging hole of its bottom in the middle of the interior gas-solid of gasifying reactor was pulsed and fallen into, and fall into thin ash or slag or the thick ash discharging hole discharge of inert bed material bottom it of peripheral air compartment.
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 that present various gasification technologies exist on high-sulfur, high ash, high ash melting point gasification:
1, reactor adopts close phase turbulent flow fluidisation section, high-density nucleolus flow sections and three sections designs of the quick flow sections of high-density, segmented gasification pressurizes under the fluidised form of different characteristics, guaranteed that coarse particles coal, fine particulate coal and sweetening agent all have the sufficient reaction times at different sections, and the mobilization dynamic feature amplification performance of these sections is good.
2, the air compartment subregion is provided with, and wind cap and peripheral fluidisation blast cap in the middle of being equipped with on the air distribution plate make that close phase turbulent flow fluidisation Duan Bufeng is even, deslagging is smooth and easy and effectively prevent high-temperature coking.
3, the production object follow-up according to gasification, vaporized chemical can adopt steam to add various ways such as air, oxygen-rich air or pure oxygen.
4, vaporized chemical adopts the mode that classification adds, and helps the reasonable distribution of temperature in the gasifier; Wherein, bottom close phase turbulent flow fluidisation section gasification temperature is lower, can prevent the too high and coking of local temperature, the quick flow sections of middle part high-density nucleolus flow sections and top high-density adopts higher reaction temperatures, help improving the efficiency of carbon conversion of gasification reaction, overcome general fluidized-bed gasification efficiency of carbon conversion weakness on the low side.
5, adopt pressurized gasification, increased substantially the gasification intensity of unit surface, dwindled the volume of gasification installation.
6, adopt the two-stage efficient cyclone separator, but the fine particle of particle diameter more than 10 microns in the high efficiency separation coal gas, and total efficiency of separation reaches more than 99%; Make the quality height of coal gas on the one hand, be particularly suitable for the gasification of dirty coal kind; High on the other hand separation efficiency has been created condition for forming high circulation ratio.
7, 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 revert pipe, add the thin bed material of a certain amount of inertia and can improve recycle stock smooth and easy in the flowing property of cyclonic separator bottom material blanking tube and returning charge, form high circulation ratio, guaranteed that high-density nucleolus flow sections and the quick flow sections of high-density have high granule density, promoted efficiency of carbon conversion to improve.
8, adopt 0～10mm wide-size distribution coal, particle size range is wide, is fit to handle the broken coal of present mechanical mining, requires lower to coal dust preparation system.
9, 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 high-density pressurized fluidized bed coal gasification apparatus overall structure synoptic diagram of the present invention.
Fig. 2 is a high-density pressurized fluidized bed coal gasification apparatus bottom construction enlarged diagram of the present invention.
Fig. 3 is a high-density pressurized fluidized bed coal gasification 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 returning charge valve 5, secondary efficient cyclone separator 6, secondary material blanking tube 7, secondary returning charge valve 8, close phase turbulent flow fluidisation section 9, high-density nucleolus flow sections 10, the quick flow sections 11 of high-density, auxiliary gasifying agent import 12, coal and Wingdale import 13, one-level returning charge mouth 14, air distribution plate 15, scum pipe 16, air compartment 17, middle wind cap 18, periphery fluidisation blast cap 19, middle air compartment 20, periphery air compartment 21, thin ash discharging hole 22, steam-in 23, main vaporized chemical import 24, thick ash discharging hole 25, one-level second gasification agent import 26, secondary second gasification agent import 27, secondary returning charge mouth 28, reactor outlet 29, one-level revert pipe 30, secondary revert pipe 31, the one-level inert bed material adds inlet 32, the secondary inert bed material adds inlet 33, thermal insulation layer 34, waste heat boiler 35, dust separation device 36, chemical production equipment 37, CFB boiler 38, well heater 39, mixing tank 40.Coal and Wingdale A, main vaporized chemical B, second gasification agent C, air or pure oxygen or oxygen-rich air 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 particle M, the thin ash of air compartment or slag or inert bed material N in the middle of advancing, advance thin ash of peripheral air compartment or slag or inert bed material O, superheated vapour P, vaporized chemical Q, Low Temperature Steam R, high-temperature steam S, low temperature purified gas T, ash discharge U, cleaned coal gas V, Chemicals W.
Embodiment
Be divided into the close fluidisation of turbulent flow mutually section 9, high-density nucleolus flow sections 10, the quick flow sections 11 of high-density referring to accompanying drawing 1 and Fig. 2 gasifying reactor 1, according to the vaporization characteristic of high-sulfur, high ash, the high-ash-fusion coal segmented gasification that pressurizes, vapor pressure is 1.0～2.5MPa.Close phase turbulent flow fluidisation section 9 is the emulsion zone of 2～5m for solids volume concentration 0.3～0.45, bed depth, adopt the turbulent flow fluidisation operation scheme of temperature 850～1050 degree, gas speed 1～1.5m/s, its function is to realize well blend and the caloic transmission of bed material, coal and Wingdale A, vaporized chemical Q and one-level returning charge H, and devolatilization, burning and the partial gasification reaction of carrying out coal; It is 0～3mm inert bed material that the bed material adopts particle diameter, as quartz sand; Coal adds from the close fluidisation of turbulent flow mutually section 9 with Wingdale A, and adopting particle diameter is the particle of 0～10mm; Vaporized chemical Q mixes for the air of the superheated vapour P of gasification required 80～93% and 100% or pure oxygen or oxygen-rich air D, the mode that vaporized chemical Q adopts classification to add, 30～50% second gasification agent C adds from the one-level second gasification agent import 26 and the secondary second gasification agent import 27 of high-density nucleolus flow sections 10, and 50～70% main vaporized chemical B adds from the main vaporized chemical import 24 of circumferential annular air compartment 21; Close phase turbulent flow fluidisation section 9 coal fugitive constituents are deviate from air or oxygen generation combustion reactions the gasification reaction heat is provided, and steam and coal generation part gasification reaction produce coal gas and semicoke then.The quick flow sections 11 of high-density nucleolus flow sections 10 and high-density is main sections of gasification reaction and desulphurization reaction, and the semicoke that generates behind close phase turbulent flow fluidisation section 9 partial gasifications is at this section gasification, the H that Wingdale produces gasification
2S removes.The quick flow sections 11 of high-density nucleolus flow sections 10 and high-density is main sections of gasification reaction and desulphurization reaction, and the semicoke that generates behind close phase turbulent flow fluidisation section 9 partial gasifications is at this section gasification, the H that Wingdale produces gasification
2S removes.The mobile operation scheme of high-density nucleolus that high-density nucleolus flow sections 10 highly is 5～8m, employing temperature 1000～1200 is spent, solids volume concentration is 0.1～0.2 gentle fast 1.5～2m/s; This section cross section is bigger, by in this section, the bottom adds second gasification agent C and the bottom adds secondary returning charge K, form the high-density nucleolus and flow, the slippage of near wall district gas-solid and back-mixing have been strengthened the interaction between the gas-solid, can improve gasification reaction and sulfurous pollutants removes speed.The quick flow sections 11 of high-density highly is 3～5m, adopts about temperature 1100 degree, solids volume concentration is greater than the high-density of the 0.1 gentle fast 2.5～3m/s operation scheme that flows fast; The fast mobile formed turbulence of sufficiently high reaction section and high-density has guaranteed the particulate profit reduction and reserving time, and efficiency of carbon conversion and pollutant removing efficient are improved.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 inert bed material etc.), making particle diameter be that particle more than 10 microns is all separated gets off, total efficiency of separation is greater than 99%, wherein the first step is greater than 95%, and the second stage is greater than 85%.Take independent returning charge mode, one-level returning charge H enters close phase turbulent flow fluidisation section 9, and secondary returning charge K enters high-density nucleolus flow sections 10, and the two-stage returning charge is not disturbed mutually; Returning charge elegance 2～5% required superheated vapour P of gasification; In addition, for improving the flowability of returning charge, in revert pipe, add the thin bed material of 200 microns following inertia of a certain amount of particle diameter, carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation with guarantee that the two-stage returning charge amounts to the high circulation ratio more than 50, make not react completely semicoke and Wingdale.The slag particle M that gasification produces is gone out by scum pipe row 16, air compartment 20 in the middle of 5～15% superheated vapour P that gasify required feed, enter gasifier 1 via middle wind cap 18, the slag particle M that gasification produces blows in the orientation of superheated vapour P and enters scum pipe 16 down smoothly, be interrupted or discharge continuously by residue extraction mechanism, this superheated vapour P also can play thermoregulatory effect, and the temperature by the amount that adds superheated vapour P is regulated air distribution plate 15 zones prevents high-temperature coking; Because the thin ash of air compartment 20 or slag or inert bed material N were discharged by the thin ash discharging hole 22 of its bottom in the middle of gasifying reactor 1 interior gas-solid was pulsed and fallen into, and fall into thin ash or slag or thick ash discharging hole 25 discharges of inert bed material O bottom it of peripheral air compartment.
Concrete structure is: gasifying reactor 1 is built by laying bricks or stones by refractory brick or refractory material casting forms, and is arranged in the pressure vessel 2, is filled with thermal insulation layer 34 between pressure vessel 2 and the gasifying reactor 1; Gasifying reactor 1 is divided into close phase turbulent flow fluidisation section 9, high-density nucleolus flow sections 10, the quick flow sections 11 of high-density from bottom to top.The top of close phase turbulent flow fluidisation section is provided with one-level returning charge mouth 14, and the bottom is provided with coal and Wingdale import 13, and the bottom is provided with air distribution plate 15 and scum pipe 16; Even for close phase turbulent flow fluidisation section 9 cloth wind, deslagging is smooth and easy and prevent high-temperature coking, wind cap 18 and peripheral fluidisation blast cap 19 in the middle of being equipped with on the air distribution plate 15; Air distribution plate 15 bottoms are air compartment 17, and air compartment 17 is made up of middle air compartment 20 and peripheral air compartment 21; Middle air compartment 20 bottoms are provided with thin ash discharging hole 22 and superheated vapour inlet 23; The side of periphery air compartment 21 is provided with main vaporized chemical import 24, and the bottom is provided with two thick ash discharging holes 25; Air compartment 20 and pressure vessel 2 led to outside the stove in the middle of scum pipe 16 passed.High-density nucleolus flow sections 10 is the amplification thorax body between close phase turbulent flow fluidisation section 9 and the quick flow sections 11 of high-density, lower side is provided with one-level second gasification agent import 26, the middle part is provided with secondary second gasification agent import 27, and secondary returning charge mouth 28 is arranged on one-level second gasification agent import 26 tops.The diameter of the quick flow sections 11 of high-density is identical with close phase turbulent flow fluidisation section 9, the reactor outlet 29 of its upper side links to each other with one-level efficient cyclone separator 3, the bottom of separator is connected to one-level material blanking tube 4, the bottom of material blanking tube is connected to one-level returning charge valve 5, one-level revert pipe 30 becomes 30～45 degree to be connected one-level returning charge mouth 14 with reactor axis, and one-level revert pipe 30 is provided with the one-level inert bed material and adds inlet 32; The outlet on one-level efficient cyclone separator 3 tops is connected to secondary efficient cyclone separator 6, with 3 one-tenth 60～90 degree of one-level efficient cyclone separator and in higher location arrangements, the bottom of separator is connected to secondary material blanking tube 7, the bottom of material blanking tube is connected to secondary returning charge valve 8, secondary revert pipe 31 becomes 30～45 degree to be connected secondary returning charge mouth 28 with reactor axis, and secondary revert pipe 31 is provided with the secondary inert bed material and adds inlet 33.
With reference to Fig. 3, the day output of implementing according to the present invention is that the detailed process of 200 tons high-sulfur, high ash, high ash melting point coal gasifying process is:
On the agent structure, gasifying reactor 1 height overall 18m, wherein close phase turbulent flow fluidisation section 9 high 5m diameter 1m, high-density nucleolus flow sections 10 high 8m diameter 1.3m, the quick flow sections 11 high 5m diameter 1m of high-density; Gasifying reactor 1 forms thick about 100mm by refractory materials (white fused alumina or brown corundum) cast; Be arranged in the pressure vessel 2, be filled with the thick thermal insulation layer of 150mm 34 (as insulating brick or aluminum silicate fiber) between pressure vessel 2 and the gasifying reactor 1; Coal and Wingdale import 13 are arranged on air distribution plate 15 top 1.5m and highly locate, and one-level returning charge mouth 14 is arranged on air distribution plate 15 top 2.5m and highly locates; 0.8m and 4m that one-level second gasification agent import 26 and secondary second gasification agent import 27 are separately positioned on high-density nucleolus flow sections 10 highly locate, and the 1m that secondary returning charge mouth 28 is arranged on this section highly locates; The raw gas outlet is arranged on the quick flow sections 11 of high-density and highly locates apart from top 0.8m.
In the concrete technical process, pass through helixes feed equipment earlier, adding granularities from the coal of close phase turbulent flow fluidisation section 9 and Wingdale import 13 is inert bed material (as the end slag of quartz sand or circulating fluidized bed) about 0～6mm, forms the emulsion zone of 4.5～5m earlier at this section; 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 24, high-temperature fuel gas is sent into peripheral air compartment 21, and high-temperature fuel gas enters close phase turbulent flow fluidisation section 9 heated inert bed material after passing the peripheral fluidisation blast cap 19 of air distribution plate 15; Adopt this moment N2 as returning charge wind earlier, start the material circulation, make in one-level material blanking tube 4, one-level returning charge valve 5 and secondary material blanking tube 7, the secondary returning charge valve 8 all to be full of a certain amount of inert bed material, and can circulate smoothly.When inert bed material is heated to 500 ℃ of left and right sides by high-temperature fuel gas, be that the coal of 0～10mm is added to the close fluidisation of turbulent flow mutually section 9 from coal and Wingdale import 13 with median size; Inert 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 bed temperature constantly raises; Superheated vapour inlet 23 in middle air compartment 20 bottoms feeds a certain amount of superheated vapour P (pressure 2.2MPa, 450 ℃ of temperature) during this time, in order to prevent the localized hyperthermia's coking of air distribution plate zone and to start deslagging; When bed temperature reaches 800 ℃ of left and right sides, stop to add high-temperature fuel gas, increase the amount (8.3 tons/hour, Ca/S ratio be 2.5) of coal and Wingdale and drop into vaporized chemical Q, the pressure of regulating gasifying reactor 1 simultaneously is to 2.0MPa, and this moment, gasifying reactor 1 interior chemical reaction was switched to pressurized gasification by the normal pressure burning; Vaporized chemical Q and coal generation part gasification reaction produce coal gas and semicoke; Vaporized chemical Q is mixed at mixing tank 40 by the superheated vapour P (pressure 2.2MPa, 450 ℃ of temperature) of gasification required 88% and 100% oxygen (pressure 2.2MPa, 600 ℃ of temperature), and pressure is about 2.2MPa, temperature is about 550 ℃; The mode that vaporized chemical Q adopts classification to add, 40% second gasification agent C adds from the one-level second gasification agent import 26 and the secondary second gasification agent import 27 of high-density nucleolus flow sections 10, and 60% main vaporized chemical B adds from the main vaporized chemical import 24 of circumferential annular air compartment 21; This moment, the returning charge wind of two-stage returning charge was used superheated vapour P instead, and total amount accounts for 3～5% of the required superheated vapour P of gasification.
After starting pressurized gasification, close phase turbulent flow fluidisation section 9, high-density nucleolus flow sections 10 are controlled at respectively with the operation scheme of the quick flow sections 11 of high-density: the close fluidisation of turbulent flow mutually section 9 is the emulsion zone of 4m for solids volume concentration 0.4, bed depth, adopts the turbulent flow fluidisation operation scheme of temperature 950 degree, gas speed 1.2m/s; High-density nucleolus flow sections 10 solids volume concentrations are 0.15, adopt the mobile operation scheme of high-density nucleolus of temperature 1150 degree, gas speed 1.8m/s; The quick flow sections solids volume concentration of high-density adopts the mobile fast operation scheme of high-density of temperature 1100 degree, gas speed 2.7m/s greater than 0.1.
The raw gas F that gasification generates separates wherein solid particulate (being mainly CaS that coke, the desulfurization completely of flying dust, unreacted produce and thin bed material etc.) through the two-stage efficient cyclone separator, make particle diameter be that particle more than 10 microns is all separated and get off, total efficiency of separation is greater than 99%; Take independent returning charge mode, the two-stage material returning device does not disturb mutually; In revert pipe, add the thin bed material of a certain amount of 100 microns following inertia and guarantee high circulation ratio more than 50, make do not react completely semicoke and Wingdale carry the removal efficiency of high-carbon transformation efficiency and sulfurous pollutants by continuous circulation.The slag particle M that gasification produces is gone out by scum pipe row 16, air compartment 20 in the middle of 5～15% superheated vapour P that gasify required feed, enter gasifier 1 via middle wind cap 18, the slag particle M that gasification produces blows in the orientation of superheated vapour P and enters scum pipe 16 down smoothly, be interrupted or discharge continuously by residue extraction mechanism, this superheated vapour P also can play thermoregulatory effect, and the temperature by the amount that adds superheated vapour P is regulated air distribution plate 15 zones prevents high-temperature coking; Because the thin ash of air compartment 20 or slag or inert bed material N were discharged by the thin ash discharging hole 22 of its bottom in the middle of gasifying reactor 1 interior gas-solid was pulsed and fallen into, and fall into thin ash or slag or thick ash discharging hole 25 discharges of inert bed material O bottom it of peripheral air compartment.
According to day output of the invention process is that the main technical details of 200 tons high-sulfur, high ash, high ash melting point coal gasification apparatus and technology is as follows: gasifying medium is pure oxygen+steam, vapor pressure 2.0MPa, 1100 ℃ on 1150 ℃ of tops, 950 ℃ of middle parts, gasifier temperature bottom, oxygen consumption 280Nm
3O
2/ 1000Nm
3(CO+H
2+ CH
4), efficiency of carbon conversion 95%, moisture-and-ash-free basis gas consumption 0.34kg/kg, moisture-and-ash-free basis coal consumption 0.65kg/Nm
3, raw gas effective constituent (CO, H
2, CH
4) 78%.
In subsequent technique, 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 35 coolings, the sensible heat of high temperature purified gas L produces Low Temperature Steam R and low temperature purified gas T after heat exchange, low temperature purified gas T becomes cleaned coal gas V behind dust separation device 36, for chemical production equipment 37 production chemical product W; The ash discharge U of dust separation device 36 and the deslagging M of gasifier 1, fall in the middle of air compartment 20 thin ash or slag or inert bed material N and fall into the thin ash of peripheral air compartment or slag or inert bed material O are discharged by the thick ash discharging hole 25 of its bottom, send into burning in the CFB boiler 38, produce high-temperature steam S, the Low Temperature Steam R that high-temperature steam S and waste heat boiler 35 produce also together again through after well heater 39 heating, becomes superheated vapour P; Superheated vapour P part chemical production equipment 37 uses, and a part is for directed deslagging usefulness, and a part is mixed the back with air or oxygen at mixing tank 38 and formed vaporized chemical Q.
Claims (2)
1. high-density pressurized fluidized bed coal gasification apparatus, it is characterized in that: gasifying reactor (1) is arranged in the pressure vessel (2), is divided into close phase turbulent flow fluidisation section (9), high-density nucleolus flow sections (10) and the quick flow sections of density (11) from bottom to top, wherein:
Close phase turbulent flow fluidisation section (9) top is provided with one-level returning charge mouth (14), the bottom is provided with coal and Wingdale import (13), the bottom is provided with air distribution plate (15) and scum pipe (16), wind cap (18) and peripheral fluidisation blast cap (19) in the middle of being equipped with on the air distribution plate (15), air distribution plate (15) bottom is air compartment (17), and air compartment (17) is made up of middle air compartment (20) and peripheral air compartment (21); Middle air compartment (20) bottom is provided with thin ash discharging hole (22) and steam-in (23), the side of periphery air compartment (21) is provided with main vaporized chemical import (24), the bottom is provided with two thick ash discharging holes (25), and air compartment (20) and pressure vessel (2) led to outside the stove in the middle of scum pipe (16) passed;
High-density nucleolus flow sections (10) is positioned between close phase turbulent flow fluidisation section (9) and the quick flow sections of high-density (11), the bottom is provided with one-level second gasification agent import (26), the middle part is provided with secondary second gasification agent import (27), and secondary returning charge mouth (28) is arranged on one-level second gasification agent import (26) top;
The diameter of the quick flow sections of high-density (11) is identical with close phase turbulent flow fluidisation section (9), the reactor outlet on its top (29) links to each other with one-level efficient cyclone separator (3), the bottom of separator is connected to one-level material blanking tube (4), the bottom of material blanking tube is connected to one-level returning charge valve (5), one-level revert pipe (30) becomes 30～45 degree to be connected one-level returning charge mouth (14) with gasifying reactor (1) axis, and one-level revert pipe (30) is provided with the one-level inert bed material and adds inlet (32); The outlet on one-level efficient cyclone separator (3) top is connected to secondary efficient cyclone separator (6), with 3 one-tenth 60～90 degree of one-level efficient cyclone separator and in higher location arrangements, the bottom of secondary efficient cyclone separator (6) is connected to secondary material blanking tube (7), the bottom of material blanking tube is connected to secondary returning charge valve (8), secondary revert pipe (31) becomes 30～45 degree to be connected secondary returning charge mouth (28) with reactor axis, and secondary revert pipe (31) is provided with the secondary inert bed material and adds inlet (33).
2. gasification process that is used for the described high-density pressurized fluidized bed coal gasification apparatus of claim 1, it is characterized in that: according to the vaporization characteristic of high-sulfur, high ash, high-ash-fusion coal, adopt the fluidised form of the different characteristics segmented gasification that pressurizes from bottom to top successively, vapor pressure is 1.0～2.5MPa; Wherein, close phase turbulent flow fluidisation section (9) adopts the turbulent flow fluidisation operation scheme of temperature 850～1050 degree, solids volume concentration 0.3～0.45 gentle fast 1～1.5m/s; It is the mobile operation scheme of high-density nucleolus of 0.1～0.2 gentle fast 1.5～2.0m/s that high-density nucleolus flow sections (10) adopts temperature 1000～1200 degree, solids volume concentration; The quick flow sections of high-density (11) adopts temperature 1100 degree, solids volume concentration greater than the mobile fast operation scheme of the high-density of 0.1 gentle fast 2.5～3m/s;
Coal joins the close fluidisation of turbulent flow mutually section (9) with Wingdale, the mode that vaporized chemical (Q) adopts classification to add, 30～50% second gasification agent (C) adds from the one-level second gasification agent import (26) and the secondary second gasification agent import (27) of high-density nucleolus flow sections (10), and 50～70% main vaporized chemical (B) adds from the main vaporized chemical import (24) of circumferential annular air compartment (21); This vaporized chemical (Q) mixes also for the air of the superheated vapour (P) of gasification required 80～93% and 100% or pure oxygen or oxygen-rich air D; The raw gas (F) that gasification generates separates with secondary efficient cyclone separator (6) by the one-level efficient cyclone separator (3) of polyphone, and total efficiency of separation is greater than 99%; The solid particulate that separates falls into material blanking tube and the returning charge valve from the device bottom, returning charge elegance 2～5% required superheated vapour P of gasification; Add the thin bed material of 200 microns following inertia of a certain amount of particle diameter in the revert pipe, amount to the high circulation ratio more than 50 to guarantee the two-stage returning charge; The slag particle (M) that gasification produces blows down to be gone out by scum pipe row (16) in the orientation of required 5～15% superheated vapours (P) of gasification, fall into the thin ash of air compartment (20) or slag or inert bed material by the interior gas-solid of gasifying reactor (1) pulsation and discharge, discharge by the thick ash discharging hole of its bottom and fall into the thin ash of peripheral air compartment or slag or inert bed material by its bottom ash discharging hole.
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| CN115234900A (en) * | 2022-06-24 | 2022-10-25 | 哈尔滨红光锅炉总厂有限责任公司 | Circulating fluidized bed hot water boiler for burning coal powder particles and burning method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2740609Y (en) * | 2004-09-10 | 2005-11-16 | 陕西秦能天脊科技有限公司 | Powdery coal gasifier of pressurized selecting ash-ejecting fluidized bed |
| WO2006064320A1 (en) * | 2004-12-16 | 2006-06-22 | Foster Wheeler Energy Corporation | Method of co-producing activated carbon in a circulating fluidized bed gasification process |
| CN1928029A (en) * | 2006-09-11 | 2007-03-14 | 东南大学 | Large-scale method and apparatus for spouted fluidized bed coal pressure gasification |
-
2008
- 2008-10-15 CN CN2008101551063A patent/CN101372635B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2740609Y (en) * | 2004-09-10 | 2005-11-16 | 陕西秦能天脊科技有限公司 | Powdery coal gasifier of pressurized selecting ash-ejecting fluidized bed |
| WO2006064320A1 (en) * | 2004-12-16 | 2006-06-22 | Foster Wheeler Energy Corporation | Method of co-producing activated carbon in a circulating fluidized bed gasification process |
| CN1928029A (en) * | 2006-09-11 | 2007-03-14 | 东南大学 | Large-scale method and apparatus for spouted fluidized bed coal pressure gasification |
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