CN101781584B - Method and equipment for gasifying coal by using plasma - Google Patents

Method and equipment for gasifying coal by using plasma Download PDF

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CN101781584B
CN101781584B CN2010101186828A CN201010118682A CN101781584B CN 101781584 B CN101781584 B CN 101781584B CN 2010101186828 A CN2010101186828 A CN 2010101186828A CN 201010118682 A CN201010118682 A CN 201010118682A CN 101781584 B CN101781584 B CN 101781584B
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gasification
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water vapor
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CN101781584A (en
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周开根
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Abstract

The invention provides method and equipment for gasifying coal, relating to a coal chemical industry technique and gasification furnace equipment. The invention is characterized in that a fluidized bed gasification furnace is designed into a three-section working mode, the upper section is a suspended preheating section, the middle section is a turbulent flow pyrolyzing section, the lower section is a bubbled gasifying section, a plasma torch is arranged at the bubbled gasifying section, and water vapor is heated to be greater than 4000 DEG C in the plasma torch, is decomposed into active chemicals H., O., H2., HO., O2. and then is directly sprayed to carbon coke of the bubbled gasifying section for chemical reaction to generate synthesis gas of CO and H2 and release heat; and pyrolysis gas, the water vapor and fluidized gas in the furnace are mixed, are discharged out of the furnace through an outlet of the suspended preheating section and then return the bubbled gasifying section of the gasification furnace through a fluidized air pipe and a fluidized fan, and soot, gaseous tar, CmHn and CH4 in the pyrolysis gas react with the water vapor to generate the synthesis gas of the CO and the H2. Compared with the conventional coal gasification technique, the invention reduces the consumption of coal resources and the discharge of greenhouse gases.

Description

The method and apparatus of gasifying coal by using plasma
Technical field
The present invention relates to coal chemical technology, specially refer to the method and gasification furnace apparatus of gasification.
Background technology
Rich coal resources in China, the virgin gas of extensive hydrogen manufacturing and production methyl alcohol, dme all passes through gasification and obtains, and conventional Coal Gasification Technology adopts the oxygen steam gasification process; The required heat of gasification reaction is provided by the oxidizing reaction of charcoal, and the vaporization rate of this coal gasification method is low, and vaporization rate is below 90%; The hydrogen mark is low in the synthetic gas that generates, and has only about 30%, makes the yielding poorly of title product; Coal system methyl alcohol technology like routine; Produce 1 ton of methyl alcohol and need consume 1.5 tons of fat coals, the coal resources that not only consume are many, and increased the greenhouse gases emission amount of carbon dioxide.
Summary of the invention
The objective of the invention is to overcome the shortcoming of existing Coal Gasification Technology, use the plasma gasification technology, coal gasifying process reasonable in design and gasification furnace apparatus realize reducing consumption of coal resources and GHG emissions mitigation.
Gasifying coal by using plasma method 1 of the present invention; Comprise the fluidized-bed gasification technology; Be to be designed to three sections mode of operation to fluidized-bed gasification furnace (1), present, in, following layout: epimere is suspension preheating section (1-IV), plays a part to make raw materials evaporate to go out water vapor and heating raw; The stage casing is turbulent flow pyrolysis section (1-III), plays raw material and continues decomposes effusion pyrolysis gas; Hypomere bubbling gasification section (1-II) plays coke and is gasified totally and generates synthetic gas and slag.Plasma torch is arranged on bubbling gasification section (1-II), with the working gas of water vapor as plasma torch, makes water vapor more than plasma torch internal heating to 4000 ℃, decomposes to generate H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the coke of bubbling gasification section (1-II), react as follows:
C(s)+4H *＝CH 4+75.6kj
C(s)+2O *＝CO 2+566kj
C(s)+2H 2 *＝CH 4+75.6kj
2C(s)+2HO *＝2CO+H 2-131.2kj
C(s)+O 2 *＝CO 2+566kj
The activity chemistry thing of water molecules and coke carry out chemical reaction and generate CO, H 2, CO 2, CH 4, and emit heat energy, subsequently CO 2Carry out reduction reaction with coke again and generate CO, (1-II) is provided with the water vapor spray gun simultaneously in the bubbling gasification section, having water vapor to participate under the situation of reaction CH 4With water vapor or CO 2Reaction generates CO and H 2The required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coke in the stove; Wherein the thermopositive reaction of activity chemistry thing and coke accounts for about 70% of total thermal discharge, and the heat release of high-temperature plasma accounts for about 30% of total thermal discharge.Fluidized wind is taken from the gasification resultant in the fluidized-bed gasification furnace (1); Outside stove under the graviational interaction of fluidized wind machine (4); Fluidized wind is operation from bottom to top in stove; The bubbling gasification section of flowing through (1-II), turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV) are drawn outside the stove by the top outlet of suspension preheating section (1-IV) again, return the air compartment (1-I) in the fluidized-bed gasification furnace (1) through fluidisation airduct a (3) and fluidisation blower fan (4) then; Get into bubbling gasification section (1-II) through the blast cap (110) on the air distribution plate (109) again; Carry out circular flow, fluidized wind is the double as perolene also, the thermal energy transfer of bubbling gasification section (1-II) to turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV).Coal dust or coal water slurry spray into the suspension preheating section (1-IV) in the fluidized-bed gasification furnace (1) by spray gun; Carry out preheating and evaporate water vapor in suspension preheating section (1-IV), the coal grain falls into turbulent flow pyrolysis section (1-III) with the free setting mode then, rolls up and down at turbulent flow pyrolysis section (1-III) and is heated; Become coke granule behind the effusion pyrolysis gas and fall into bubbling gasification section (1-II); At bubbling gasification section (1-II), coke granule moves up and down with the bubbling fluidization mode, and the activity chemistry thing that sprays with plasma gun carries out chemical reaction; Reach with water vapor and carry out chemical reaction, generate CO and H 2Synthetic gas, become molten slag until being gasified totally and enter the water seal slag bath.The pyrolysis gas that generates at turbulent flow pyrolysis section (1-III) mixes with fluidized wind; Enter into suspension preheating section (1-IV); The water vapor that generates with suspension preheating section (1-IV) mixes again; Outlet is drawn outside the stove through the top of suspension preheating section (1-IV), enters in the bubbling gasification section (1-II) with the air compartment (1-I) and the blast cap (110) on the air distribution plate (109) of fluidisation blower fan (4), fluidized-bed gasification furnace (1) through fluidisation airduct a (3), and water vapor wherein and coke carry out chemical reaction generation CO and H 2, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Generate in the fluidized-bed gasification furnace (1) with CO and H 2For the syngas mixture of staple is come out by the syngas outlet on bubbling gasification section (1-II) top; Getting into gas-solid separator (6) separates; Isolated carbon granule returns the bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) and carries out gasification process, and isolated synthetic gas carries out dedusting, desulfurizing and purifying processing after reclaiming the heat cooling through waste heat boiler again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.
In the above-mentioned method 1; Working pressure in the fluidized-bed gasification furnace (1) is controlled between 0～5kPa; The service temperature of suspension preheating section (1-IV) is controlled between 270～330 ℃; The service temperature of turbulent flow pyrolysis section (1-III) is controlled between 750～850 ℃, and the service temperature of bubbling gasification section (1-II) is controlled between 1100～1200 ℃, and working pressure and service temperature are controlled through the output flow of adjusting synthetic gas and the electric power of plasma torch and the input of water vapor in the stove.Through the reducing design, make fluidized wind be designed to three sections wind speed in the fluidized-bed gasification furnace (1), the mean wind speed of bubbling gasification section (1-II) is 1～2.5m/s, and the wind speed of turbulent flow pyrolysis section (1-III) is 3～5m/s, and the wind speed of suspension preheating section (1-IV) is 1～2m/s.In present method; Spray in the suspension preheating section (1-IV) of fluidized-bed gasification furnace (1) as gasified raw material with coal dust or coal water slurry; The residence time of gasified raw material in stove is greater than 15min; When with coal dust during as gasified raw material, the particle diameter of coal dust is 30～150 μ m, simultaneously the water vapor vaporized chemical of input coal dust weight 60～85% in stove; Be sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, 45% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II); When with coal water slurry during as gasified raw material; The ratio of moisture is 30～40% in the coal water slurry; The particle diameter of coal is less than 50 μ m; In stove, add the water vapor vaporized chemical of coal water slurry total amount 45% simultaneously, wherein 80% of water vapor vaporized chemical addition through being sprayed on the coke in the bubbling gasification section (1-II) after the plasma torch decomposition activation, and 20% of water vapor vaporized chemical addition is directly imported in the bubbling gasification section (1-II).In present method, use conventional operative technique and spray into coal dust or coal water slurry raw material in the fluidized-bed gasification furnace.
In the above-mentioned method 1; Heat exchanger (8) and gas-solid separator (6) are set in the periphery of vapourizing furnace; Fluidized wind in the fluidized-bed gasification furnace (1) is taken pyrolysis G&W steam and is drawn outside the stove by the top of suspension preheating section (1-IV); Through fluidisation airduct a (3), fluidisation blower fan (4) sub-air chamber (803), enter into collection chamber (815) through heat exchanger tube (810) more then, make the fluidized wind intensification of through heat exchanger tube (810) time, being heated indirectly with fluidisation airduct b (5) entering heat exchanger (8); Come out by collection chamber outlet (814) then, the air compartment (1-I) through pipe connecting a (28), fluidized-bed gasification furnace (1) returns bubbling gasification section (1-II); The synthetic gas that generates in the fluidized-bed gasification furnace (1) is come out by the syngas outlet on bubbling gasification section (1-II) top; Getting into gas-solid separator (6) through pipe connecting b (29) separates; Isolated charcoal ash returns the bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) and carries out gasification process; Isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8), gives the fluidized wind in the heat exchanger tube (810) the heat indirect exchange, is come out by heat exchange chamber (809) then; After the cooling of waste heat boiler recovery heat, send into subsequent handling and handle.
A kind of gasifying coal by using plasma equipment of realizing aforesaid method 1 of the present invention; It is characterized in that fluidized-bed gasification furnace (1) is made up of suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I); Suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I) are in same solid of revolution furnace wall; Present between suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III) and the bubbling gasification section (1-II), in, following layout and directly communicating, suspension preheating section (1-IV) is at epimere, turbulent flow pyrolysis section (1-III) is in the stage casing; Bubbling gasification section (1-II) is at hypomere; Be air compartment (1-I) below the bubbling gasification section (1-II), between bubbling gasification section (1-II) and the air compartment (1-I) air distribution plate (109) arranged, blast cap (110) is arranged on the air distribution plate (109); The slag notch of bubbling gasification section (1-II) is arranged on the outer periphery of air distribution plate (109), and slag notch is layout in the form of a ring; Plasma torch and water vapor spray gun are installed on the furnace wall of bubbling gasification section (1-II); On the furnace wall on the top of suspension preheating section (1-IV), there is fluidized wind outlet (103) to pick out, on the furnace wall at 1/2 following position of suspension preheating section (1-IV), pulverized coal gun or coal water slurry spray gun (123) access arranged; On the furnace wall on bubbling gasification section (1-II) top, there is syngas outlet to pick out; On the furnace wall of air compartment (1-I), there is fluidized wind import (108) to insert.The bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) adopts heart-shaped design; Plasma torch on bubbling gasification section (1-II) furnace wall is the multilayer layout; Every layer of ring-type is provided with many plasma torchs; The spout of plasma torch points to the stove inner axes, and the water vapor spray gun is set between the interval of plasma torch, and the water vapor spray gun is more than one at least one.In this equipment, the solid of revolution furnace wall of fluidized-bed gasification furnace (1) is made up of fire-resistant furnace wall a (120), thermal insulation layer a (121) and Steel Sheel a (122), wherein between the fire-resistant furnace wall a (120) of bubbling gasification section (1-II) and the thermal insulation layer a (121) cooling layer a (115) is arranged.Adopt the reducing design in the fluidized-bed gasification furnace (1); The internal diameter of suspension preheating section (1-IV) is 1.5 times of turbulent flow pyrolysis section (1-III); The mean inside diameter of bubbling gasification section (1-II) is 1.3 times of turbulent flow pyrolysis section (1-III) diameter; The aspect ratio of suspension preheating section (1-1V), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) is 1.5: 1.3: 1, through the reducing design, makes the interior fluidising air velocity of vapourizing furnace meet the processing requirement of aforesaid method 1; The slag notch of bubbling gasification section (1-II) is communicated to air compartment (1-I) through slagging channel (111), is water seal (107) below the air compartment (1-I), during the equipment operation; Slag falls into water seal through air compartment (1-I); Utilize the waste heat heating fluidized wind of slag, the slag falls entry generation water vapor of being honored as a queen, water vapor enters into bubbling gasification section (1-II) with fluidized wind and does the vaporized chemical utilization; Can reduce the input of the outer water vapor of stove, save the energy.Peripherals at fluidized-bed gasification furnace (1) also has fluidisation blower fan (4), heat exchanger (8), gas-solid separator (6) and waste heat boiler (10); Fluidized wind on the furnace wall of suspension preheating section (1-IV) top outlet (103) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber of heat exchanger (8) exports (814) are connected to fluidized-bed gasification furnace air compartment (1-I) through pipe connecting a (28) fluidized wind import (108); Syngas outlet on the furnace wall of bubbling gasification section (1-II) top is connected to the synthetic gas import of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down interface (104) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fluidized-bed gasification furnace bubbling gasification section (1-II); The syngas outlet of gas-solid separator (6) is connected to the synthetic gas import of heat exchanger (8) through pipe connecting d (7); The syngas outlet of heat exchanger (8) is connected to the synthetic gas import of waste heat boiler (10) through pipe connecting e (9), and the syngas outlet of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14).
Gasifying coal by using plasma method 2 of the present invention comprises the fixed bed gasification technology, is to be designed to two sections mode of operation to fixed-bed gasification furnace (2); Go to upper and lower layout, epimere is pyrolysis section (2-II), and hypomere is gasification section (2-I); Plasma torch is arranged on gasification section (2-I); With the working gas of water vapor as plasma torch, water vapor is heated in plasma torch more than 4000 ℃, decomposes to generate H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the coke of gasification section (2-I), react as follows:
C(s)+4H *＝CH 4+75.6kj
C(s)+2O *＝CO 2+566kj
C(s)+2H 2 *＝CH 4+75.6kj
2C(s)+2HO *＝2CO+H 2-131.2kj
C(s)+O 2 *＝CO 2+566kj
The activity chemistry thing of water molecules and coke carry out chemical reaction and generate CO, H 2, CO 2, CH 4, and emit heat energy, subsequently CO 2Carry out reduction reaction with coke again and generate CO, (2-I) is provided with the water vapor spray gun simultaneously in gasification section, having water vapor to participate under the situation of reaction CH 4With water vapor or CO 2Reaction generates CO and H 2The required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coke in the stove; Wherein the thermopositive reaction of activity chemistry thing and coke accounts for about 70% of total thermal discharge, and the heat release of high-temperature plasma accounts for about 30% of total thermal discharge.Coal cinder gets in the fixed-bed gasification furnace (2) space of filling gasification section (2-I) and pyrolysis section (2-II), voidage about 40% by the opening for feed of furnace roof; Space between coal cinder is as the gas channel of heat-carrying gas; Part in the gaseous state thing that the interior gasification of gasification section (2-I) generates is as heat-carrying gas, and under the graviational interaction of fluidized wind machine (4), the heat-carrying gas in the stove is moved to pyrolysis section (2-II) by gasification section (2-I) outside stove; Be delivered to pyrolysis section (2-II) to the heat of gasification section (2-I); The coal cinder of stove is gone in heating, and makes the coal cinder effusion water vapor and the pyrolysis gas of pyrolysis section (2-II), becomes coke behind coal cinder effusion water vapor and the pyrolysis gas and gets into gasification section (2-I); Water vapor, pyrolysis gas that pyrolysis section (2-II) generates mix with heat-carrying gas; Pyrolysis gas outlet (204) by pyrolysis section (2-II) top is drawn outside the stove; Get into the sub-air chamber (803) of heat exchanger (8) then through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5); Enter into collection chamber (815) through heat exchanger tube (810) again, make the intensification of through heat exchanger tube (810) time, being heated indirectly of heat-carrying mixed gas, come out by collection chamber outlet (814) then; In pipe connecting a (28) returned the gasification section (2-I) of fixed-bed gasification furnace (2), water vapor wherein and coke carried out chemical reaction and generate CO and H 2, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Form slag behind the coke gasification in the gasification section (2-I) and enter slag bath through slag notch, water seal; Generate in the fixed-bed gasification furnace (2) with CO and H 2For the synthetic gas of staple is drawn by the syngas outlet on gasification section (2-I) top; Get into gas-solid separator (6) through pipe connecting b (29) and separate, isolated charcoal ash returns the gasification section (2-I) of fixed-bed gasification furnace (2) and carries out gasification process, and isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8); Give the heat-carrying mixed gas in the heat exchanger tube (810) the heat indirect exchange; Draw by heat exchange chamber (809) then, after the cooling of waste heat boiler recovery heat, carry out dedusting, desulfurizing and purifying processing again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.
In the above-mentioned method 2; Working pressure in the fixed-bed gasification furnace (2) is controlled between negative pressure 30Pa～malleation 500Pa; Service temperature in the gasification section (2-I) is controlled between 1000～1500 ℃; Service temperature in the pyrolysis section (2-II) is controlled between 300～1000 ℃, and working pressure and service temperature are controlled through the output flow of adjusting synthetic gas and the electric power of plasma torch and the input of water vapor in the stove; The coal cinder particle diameter that is input in the stove is 20～30mm, and the residence time of coal cinder in stove is greater than 45min; In stove, import the water vapor vaporized chemical of coal cinder weight 60～85% simultaneously; Be sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, 45% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II).
A kind of gasifying coal by using plasma equipment of realizing aforesaid method 2 of the present invention; It is characterized in that fixed-bed gasification furnace (2) is made up of pyrolysis section (2-II) and gasification section (2-I); Pyrolysis section (2-II) and gasification section (2-I) are in same solid of revolution furnace wall, and pyrolysis section (2-II) and gasification section (2-I) go to upper and lower layout and directly communicate, and pyrolysis section (2-II) is at epimere; Gasification section (2-I) is provided with plasma torch and water vapor spray gun at hypomere on the furnace wall of gasification section (2-I); On the furnace wall on pyrolysis section (2-II) top, there is pyrolysis gas outlet (204) to pick out; On the furnace wall of gasification section (2-I) and pyrolysis section (2-II) combining site, there is syngas outlet to pick out, on the furnace wall of gasification section (2-I), has pyrolysis gas to melt down import (208) respectively and melt down import (209) access with the charcoal ash; The opening for feed of fixed-bed gasification furnace (2) is arranged on the furnace roof; Pyrolysis gas outlet (204) on the pyrolysis section (2-II) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber outlet (814) of heat exchanger (8) is melted down import (208) through the pyrolysis gas that pipe connecting a (28) is connected to fixed-bed gasification furnace gasification section (2-I); Syngas outlet on the furnace wall of gasification section (2-I) top is connected to the synthetic gas import of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down import (209) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fixed-bed gasification furnace gasification section (2-I); The syngas outlet of gas-solid separator (6) is connected to the synthetic gas import of heat exchanger (8) through pipe connecting d (7); The syngas outlet of heat exchanger (8) is connected to the synthetic gas import of waste heat boiler through pipe connecting e (9), and the syngas outlet of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14).
In the gasifying coal by using plasma equipment of above-mentioned realization aforesaid method 2; The solid of revolution furnace wall of fixed-bed gasification furnace (2) is made up of fire-resistant furnace wall b (218), thermal insulation layer b (219) and Steel Sheel b (220), wherein between the fire-resistant furnace wall b (218) of gasification section (2-I) and the thermal insulation layer b (219) cooling layer b (215) is arranged; Gasification section (2-I) furnace wall is designed to the back taper solid of revolution; On the back taper solid of revolution furnace wall of gasification section (2-I), many plasma torchs are set; Plasma torch is multilayer ring-type layout; Spout points to the axle center, and the water vapor spray gun is set between the interval of plasma torch, and the water vapor spray gun is more than one at least one.Coal cinder enters into fixed-bed gasification furnace (2) through carbonic acid gas sealing gland feeding unit; The carbonic acid gas sealing gland can stop air to get into vapourizing furnace through opening for feed and stop simultaneously that synthetic gas releases outside the stove through opening for feed in the stove; And it is without hindrance to charging; Carbonic acid gas sealing gland feeding unit is made up of coal hopper (3005), closed scraper plate coal conveyor (30); Wherein, carbonic acid gas sealing gland (3008) is arranged in the coal hopper (3005), going up in addition in coal hopper (3005), carbonic acid gas replenishes mouthful (3006), carbonic acid gas detects mouthful (3007); Closed scraper plate coal conveyor (30) is made up of driving wheel (3002), follow-up pulley, material loading scraper plate (3001), dividing plate (3010), backhaul scraper plate (3011) and closed shell (3009); The opening for feed (3003) of closed scraper plate coal conveyor (30) is at top; Scraper conveyor discharge port (3012) endways; Opening for feed (3003) weighing apparatus of the discharge port of coal hopper (3005) and closed scraper plate coal conveyor connects, and scraper conveyor discharge port (3012) connects with opening for feed (201) weighing apparatus of fixed-bed gasification furnace.
In aforesaid method of the present invention and the equipment, take a water vapor more than plasma torch internal heating to 4000 ℃, to decompose and generate H *, O *, H 2 *, HO *, O 2 *Inject directly on the measure on the gasification section coke behind the activity chemistry thing; Generation heat when being characterized in reacting can make the temperature of reflecting point reach more than 5500 ℃; And the room temperature of gasification section still is in 1100 ℃ of low relatively TRs; Thereby ash fusion point all is suitable in the coal more than 1100 ℃ makes gasified raw material, the coke granule of reflecting point is a molten slag by gasification and melting rapidly, the high temperature heat of reflecting point is fluidized and distributes subsequently; Can not make unreacted coke granule coking, can not make the interior temperature of stove exceed the use temperature scope of body of heater material yet; The pyritous molten slag makes steam turn to steam after falling into water seal, and water vapor gets into vaporizer and has an effect as vaporized chemical, and the heat energy in the stove can not run off.The present invention adopts bubbling fluidized bed or fixed bed pattern that gasification section is reached more than 50% near the coke dutycycle at furnace wall place in gasification section, makes the activity chemistry thing of plasma gun be easy to be ejected on the coke, helps taking place above-mentioned reaction.Through above-mentioned measure; The different steps of raw material in gasification all carried out in suitable fluidized state and service temperature; The raw material of different states can not mix, and can make the gasification section that the energy high concentration is the highest in the need temperature and heat dissipation is maximum, reasonably is assigned to pyrolysis section and preheating section to heat energy through fluidized wind or heat-carrying gas then; Obtain power consumption that reduces plasma torch and the double effects that improves the material gasification rate; Vaporization rate almost reaches 100%, and with respect to the mode that coal dust gasifies in argon-arc plasma field, the power consumption of present method can reduce about 70%.All adopt water vapor to make vaporized chemical in the gasification, from water molecules, decomposite hydrogen, the hydrogen fraction scale in the synthetic gas of coming out of the stove is increased more than 20%, carbonic acid gas reduces about 17%.
The invention has the beneficial effects as follows: raw material is widely used; Ash fusion point all can be used as gasified raw material at the coal more than 1100 ℃, almost is suitable for all coals, using plasma Coal Gasification Technology; Vaporization rate exceeds 10% than routine techniques; Hydrogen mark in the synthetic gas exceeds more than 20% than routine techniques, when the synthetic gas that generates with the gasifying coal by using plasma technology is used to produce the virgin gas of methyl alcohol, reduces coal consumption about 40%, reducing emission of carbon dioxide about 45% than routine techniques.
Description of drawings
The present invention provides attached drawings to be further described, but each accompanying drawing and following embodiment all are not construed as limiting the invention:
Fig. 1 is a kind of fluidized-bed gasifying coal by using plasma system device structure iron of the present invention;
Fig. 2 is the A-A sectional view of Fig. 1;
The B-B sectional view of Fig. 1 of Fig. 3;
Fig. 4 is a kind of fixed bed gasifying coal by using plasma system device structure iron of the present invention.
Among the figure: 1. fluidized-bed gasification furnace, 2. fixed-bed gasification furnace, 3. fluidisation airduct a, 4. fluidisation blower fan, 5. fluidisation airduct b, 6. gas-solid separator; 7. pipe connecting d, 8. heat exchanger, 9. pipe connecting e, 10. waste heat boiler, 11. pipe connectings, 12. valves; 13. induced draft fan, 14. synthetic gas transfer limes, 15. valves, 16. pipe connectings, 17. pipe connectings, 18. soot-blowing wind machines; 19. valve, 20. valves, 21. valves, 22. charcoals ash transfer lime, 23. pipe connectings, 24. pipe connectings; 25. valve, 26. pipe connectings, 27. pipe connecting c, 28. pipe connecting a, 29. pipe connecting b, 30. closed scraper plate coal conveyors; 101. furnace top cover, 102. louvers keep off grey device, the outlet of 103. fluidized winds, and 104. charcoal ashes melt down interface, 105. entrance of cooling water; 106. furnace foundation, 107. water seals, 108. fluidized wind imports, 109. air distribution plates, 110. blast caps; 111. slagging channel, 112. plasma torchs, 113. water vapor spray guns, 114. plasma torchs, 115. cooling layer a; 116. the cooling backwater outlet, 117. TPs, 118. syngas outlet, 119. TPs, 120. fire-resistant furnace wall a; 121. thermal insulation layer a, 122. Steel Sheel a, 123. pulverized coal guns or coal water slurry spray gun, 124. TPs, 125. explosive doors; 126. cooling layer lower collecting box pipe, 1-I. air compartment, 1-II. bubbling gasification section, 1-III. turbulent flow pyrolysis section, 1-IV. suspension preheating section; 201. opening for feed, 202. explosive doors, 203. louvers keep off grey device, 204. pyrolysis gas outlets, the outlet of 205. cooling backwaters; 206. water seal, 207. slagging channels, 208. pyrolysis gas melt down import, and 209. charcoal ashes melt down import, 210. furnace foundations; 211. entrance of cooling water, 212. plasma torchs, 213. water vapor spray guns, 214. plasma torchs, 215. cooling layer b; 216. TP, 217. syngas outlet, 218. fire-resistant furnace wall b, 219. thermal insulation layer b; 220. Steel Sheel b, 221. TPs, 2-I. gasification section, 2-II. pyrolysis section; 601. syngas outlet, the outlet of 602. charcoals ash, 603. synthetic gas imports; 801. sub-air chamber's import, 802. synthetic gas imports, 803. sub-air chamber, 804. upper spacers; 805. syngas outlet, 806. heat exchange chamber sidewalls, 807. thermal insulation layers, 808. shells; 809. heat exchange chamber, 810. heat exchanger tubes, 811. ash discharging holes, 812. blow the ash mouth; 813. lower clapboard, the outlet of 814. collection chambers, 815. collection chambers, 816. ash discharging holes; 1001. the synthetic gas import, 1002. syngas outlet; 1301. syngas outlet; 3001. the material loading scraper plate, 3002. driving wheels, 3003. opening for feeds, 3004. coal cinders; 3005. coal hopper, 3006. carbonic acid gas replenish mouth, and 3007. carbonic acid gas detect mouth, 3008. carbonic acid gas sealing glands; 3009. closed shell, 3010. dividing plates, 3011. backhaul scraper plates, 3012. scraper conveyor discharge ports.
Embodiment
Among embodiment 1 embodiment shown in Figure 1; Fluidized-bed gasifying coal by using plasma system is made up of fluidized-bed gasification furnace (1), fluidisation blower fan (4), heat exchanger (8), gas-solid separator (6), waste heat boiler (10), soot-blowing wind machine (18) and connecting tube; Wherein: suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I) are arranged in the fluidized-bed gasification furnace (1); Suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I) are in same solid of revolution furnace wall; The solid of revolution furnace wall is made up of fire-resistant furnace wall a (120), thermal insulation layer a (121) and Steel Sheel a (122); Between the fire-resistant furnace wall a (120) of bubbling gasification section (1-II) and thermal insulation layer a (121), cooling layer a (115) is arranged, fire-resistant furnace wall a (120) builds by laying bricks or stones with alumina firebrick or luminite cement concrete placement, and thermal insulation layer a (121) selects the aluminosilicate refractory fiber material for use; Cooling layer a (115) is made up of straight steel pipe, last circular arc header tube and following circular arc header tube; Connect with steel plate between the sidewall of straight steel pipe, the last end interface of straight steel pipe inserts goes up the circular arc header tube, and the following end interface of straight steel pipe inserts circular arc header tube (126) down; Last circular arc header tube has cooling backwater outlet (116) to pick out; Following circular arc header tube has entrance of cooling water (105) to insert, logical recirculated cooling water in the steel pipe of cooling layer a (115), and steel pipe external application refractory mortar is filled; Sub-air chamber (803), heat exchanger tube (810), collection chamber (815) and heat exchange chamber (809) are arranged in the cylinder of heat exchanger (8); Top is sub-air chamber (803); The middle part is heat exchange chamber (809); The bottom is collection chamber (815); Isolate with upper spacer (804) between sub-air chamber (803) and the heat exchange chamber (809), isolate with lower clapboard (813) between heat exchange chamber (809) and the collection chamber (815), heat exchanger tube (810) places among the heat exchange chamber (809) and through between upper spacer (804) and the lower clapboard (813); The inboard of heat exchanger tube (810) is the passage that connects between sub-air chamber (803) and the collection chamber (815), and the outside of heat exchanger tube (810) is heat exchange chamber (809); Inlet mouth (801) is arranged on the barrel of sub-air chamber (803); Air outlet (814) is arranged on the barrel of collection chamber (815); The bottom of heat exchange chamber barrel (806) one sides is provided with synthetic gas import (802), and ash discharging hole (811) is set below synthetic gas import (802), on the top of barrel (806) opposite side of heat exchange chamber syngas outlet (805) is set; Blow ash mouthful (812) in the opposite side setting of heat exchange chamber ash discharging hole (811); There are thermal insulation layer (807) and shell (808) in the cylinder outside of heat exchanger (8), and during the equipment operation, sub-air chamber (803), heat exchanger tube (810) and collection chamber (815) are as the passage of fluidized wind or heat-carrying mixed gas; Heat exchange chamber (809) is as the passage of synthetic gas, and the high-temperature synthesis gas in the heat exchange chamber (809) is conducted heat to fluidized wind or heat-carrying mixed gas through the interval of heat exchanger tube (810).Present between suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III) and the bubbling gasification section (1-II) in the fluidized-bed gasification furnace (1), in, time layout and directly communicating; Suspension preheating section (1-IV) is at epimere; Turbulent flow pyrolysis section (1-III) is in the stage casing; Bubbling gasification section (1-II) is at hypomere, is air compartment (1-I) below the bubbling gasification section (1-II), and the internal diameter of suspension preheating section (1-IV) is 2.25m, highly is 4.5m; The internal diameter of turbulent flow pyrolysis section (1-III) is 1.5m, highly for 3.9m, the mean inside diameter of bubbling gasification section (1-II) is 2m, highly is 3m; Between bubbling gasification section (1-II) and the air compartment (1-I) air distribution plate (109) is arranged; There is the slag notch of blast cap (110) bubbling gasification section (1-II) to be arranged on the outer periphery of air distribution plate (109) on the air distribution plate (109); Slag notch is layout in the form of a ring; Slag notch is communicated to air compartment (1-I) through slagging channel (111), is water seal (107) below the air compartment (1-I); Bubbling gasification section (1-II) adopts heart-shaped design; Plasma torch and water vapor spray gun are installed on the furnace wall of bubbling gasification section (1-II), and plasma torch is the multilayer layout, and the upper strata ring-type is provided with 8 plasma torchs; The spout of plasma torch points to the stove inner axes; Middle two layers are provided with 8 plasma torchs, between the interval of middle two layers of plasma torch, 7 water vapor spray guns are set, and lower floor is provided with 6 plasma torchs; Pulverized coal gun (123) is arranged on the position, middle and lower part of suspension preheating section (1-IV), and the opening for feed of pulverized coal gun (123) and coal dust feeder system weighing apparatus connect; Fluidized wind outlet (103) is arranged on the furnace wall of suspension preheating section (1-IV) top; In the ingress of fluidized wind outlet (103) louver is set and keeps off grey device (102); Fluidized wind outlet (103) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber of heat exchanger (8) exports (814) are connected to fluidized-bed gasification furnace air compartment (1-I) through pipe connecting a (28) fluidized wind import (108); Syngas outlet (118) on the furnace wall of bubbling gasification section (1-II) top is connected to the synthetic gas import (603) of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down interface (104) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fluidized-bed gasification furnace bubbling gasification section (1-II); The syngas outlet (601) of gas-solid separator (6) is connected to the synthetic gas import (802) of heat exchanger (8) through pipe connecting d (7); The syngas outlet (805) of heat exchanger (8) is connected to the synthetic gas import (1001) of waste heat boiler (10) through pipe connecting e (9), and the syngas outlet (1301) of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14); The ash discharging hole of heat exchanger (811) is connected to charcoal ash transfer lime (22) through pipe connecting (24), valve (25) and pipe connecting (26); At charcoal ash transfer lime (22) the other end soot-blowing wind machine (18) is set, heat exchange chamber blow ash mouthful (812) is connected to soot-blowing wind machine (18) air outlet one side through pipe connecting (11) and valve (12) the grey transfer lime (22) of charcoal; Collection chamber (815) at heat exchanger also has ash discharging hole (816); Ash discharging hole (816) is connected to charcoal ash transfer lime (22) through valve (20) and pipe connecting (23); Between the tie point of the tie point of pipe connecting (23) and pipe connecting (11), valve (21) is arranged; During the equipment operation, the charcoal ash of heat exchange chamber (809) drains into charcoal ash transfer lime (22) through ash discharging hole (811), pipe connecting (24), valve (25) and pipe connecting (26), returns in the vapourizing furnace through charcoal ash transfer lime (22) again; The soot-blowing wind of soot-blowing wind machine (18) air outlet is respectively charcoal ash transfer lime (22) ash discharge and is heat exchange chamber (809) ash discharge through the switching between valve (12) and the valve (21), and soot-blowing wind is taken from the synthetic gas in the synthetic gas transfer lime (14); The entrance of cooling water (105) of cooling layer a (115) the lower collecting box pipe of fluidized-bed gasification furnace (1) is connected to the water supply network of water coolant, and the backwater outlet (116) of cooling layer a (115) upper header pipe is connected to the steam water interface interface (not shown) of waste heat boiler.Plasma torch is non-transferred arc mode; Working gas interface, coolant interface and power interface (not shown) are arranged on the plasma torch; The working gas interface of plasma torch is connected to through valve and gas pipeline on the steam pipe system of waste heat boiler, adopts silica tube or vitrified pipe to do insulation at the gas pipeline near one section 50cm length of plasma torch and isolates (not shown); The refrigerant of plasma torch adopts zero(ppm) water or transformer oil; Coolant inlet arrives the coolant feed pump outlet through pipe connection; The refrigerant of plasma torch returns outlet and arrives heat abstractor through pipe connection; Adopt silica tube or vitrified pipe to do insulation at the main coolant pipe near one section 50cm length of plasma torch and isolate (not shown), the power interface of plasma torch is connected to plasma electrically source controller (not shown); The steam input interface of water vapor spray gun is connected to (not shown) on the steam pipe system of boiler through valve.TP (117) is installed on the furnace wall of bubbling gasification section (1-II); TP (119) is installed on the furnace wall of turbulent flow pyrolysis section (1-III); TP (124) is installed on the furnace wall of suspension preheating section (1-IV), also has explosive door (125) on the top furnace wall of suspension preheating section (1-IV).
The above embodiments 1 are when operation; With coal dust as gasified raw material; The particle diameter of coal dust is 30～150 μ m; In stove, import the water vapor vaporized chemical of coal dust weight 60～85% simultaneously; Be sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, 27% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II) through the water vapor spray gun, and 18% of water vapor vaporized chemical is produced, directly imports in the bubbling gasification section (1-II) with fluidized wind in the heat release of water seal slag bath by high-temperature slag; The required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coal in the stove; Fluidized wind is taken from the gasification resultant in the fluidized-bed gasification furnace (1); Under the graviational interaction of fluidized wind machine (4), fluidized wind is operation from bottom to top in stove, the bubbling gasification section of flowing through (1-II), turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV) outside stove; Draw outside the stove by the top outlet of suspension preheating section (1-IV) again; Return the air compartment (1-I) in the fluidized-bed gasification furnace (1) through the outer device of stove then, get into bubbling gasification section (1-II) through the blast cap (110) on the air distribution plate (109) again, carry out circular flow; Fluidized wind is the double as perolene also, the thermal energy transfer of bubbling gasification section (1-II) to turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV).Coal dust or coal water slurry spray into the suspension preheating section (1-IV) in the fluidized-bed gasification furnace (1) by spray gun; Carry out preheating and evaporate water vapor in suspension preheating section (1-IV); The coal grain falls into turbulent flow pyrolysis section (1-III) with the free setting mode then, rolls up and down at turbulent flow pyrolysis section (1-III) and is heated, and becomes coke granule behind the effusion pyrolysis gas and falls into bubbling gasification section (1-II); At bubbling gasification section (1-II); Coke granule moves up and down with the bubbling fluidization mode, more than plasma torch internal heating to 4000 ℃, decomposes water vapor to generate H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the interior coke of stove H *, O *, H 2 *, HO *, O 2 *Carry out chemical reaction with coke, generate CO and H 2Synthetic gas, simultaneously spray into bubbling gasification section (1-II) to water vapor through the water vapor spray gun, make water vapor and coke gasification reaction generation CO and H 2Synthetic gas, water vapor and CH 4Reaction generates CO and H 2Synthetic gas, being gasified totally until coke becomes molten slag and enters the water seal slag bath, the water vapor that slag produces in the heat release of water seal slag bath gets into bubbling gasification section (1-II) with fluidized wind and does the vaporized chemical utilization; The pyrolysis gas that generates at turbulent flow pyrolysis section (1-III) mixes with fluidized wind; Enter into suspension preheating section (1-IV); The water vapor that generates with suspension preheating section (1-IV) mixes again, draws outside the stove through the outlet of the top of suspension preheating section (1-IV), gets into the sub-air chamber (803) of heat exchanger (8) then through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5); Enter into collection chamber (815) through heat exchanger tube (810) again; Make the fluidized wind intensification of through heat exchanger tube (810) time, being heated indirectly, come out by collection chamber outlet (814) then, the stove air compartment (1-I) through pipe connecting a (28), fluidized-bed gasification furnace (1) returns bubbling gasification section (1-II); In bubbling gasification section (1-II), water vapor wherein and coke carry out chemical reaction and generate CO and H 2, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Synthetic gas; The synthetic gas that generates in the fluidized-bed gasification furnace (1) is come out by the top of bubbling gasification section (1-II); Get into gas-solid separator (6) through pipe connecting b (29) and separate, isolated charcoal ash returns the bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) and carries out gasification process, and isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8); Give the fluidized wind in the heat exchanger tube (810) the heat indirect exchange; Come out by heat exchange chamber (809) then, after the cooling of waste heat boiler recovery heat, carry out dedusting, desulfurizing and purifying processing again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.Above-mentioned in service; Working pressure in the fluidized-bed gasification furnace (1) is controlled between 0～5kPa; The service temperature of suspension preheating section (1-IV) is controlled between 270～330 ℃, and the service temperature of turbulent flow pyrolysis section (1-III) is controlled between 750～850 ℃, and the service temperature of bubbling gasification section (1-II) is controlled between 1100～1200 ℃; The mean wind speed of bubbling gasification section (1-II) is 1～2.5m/s; The wind speed of turbulent flow pyrolysis section (1-III) is 3～5m/s, and the wind speed of suspension preheating section (1-IV) is 1～2m/s, makes the residence time of raw material in stove greater than 15min; Working pressure and service temperature are controlled through the output flow of adjusting synthetic gas and the electric power of plasma torch and the input of water vapor in the stove.
In the above embodiments 1; When with coal water slurry during as gasified raw material; The ratio of moisture is 30～40% in the coal water slurry, and the particle diameter of coal adds the water vapor vaporized chemical of coal water slurry total amount 45% simultaneously less than 50 μ m in stove; Wherein 80% of water vapor vaporized chemical addition through being sprayed on the coke in the bubbling gasification section (1-II) after the plasma torch decomposition activation, and 20% of water vapor vaporized chemical addition is directly imported in the bubbling gasification section (1-II).
Among embodiment 2 embodiment shown in Figure 4; Fixed bed gasifying coal by using plasma system is made up of fixed-bed gasification furnace (2), fluidisation blower fan (4), heat exchanger (8), gas-solid separator (6), waste heat boiler (10), soot-blowing wind machine (18) and connecting tube; Wherein: pyrolysis section (2-II) and gasification section (2-I) are arranged in the fixed-bed gasification furnace (2), and pyrolysis section (2-II) and gasification section (2-I) are in same solid of revolution furnace wall, and the solid of revolution furnace wall is made up of fire-resistant furnace wall b (218), thermal insulation layer b (219) and Steel Sheel b (220); Wherein between the fire-resistant furnace wall b (218) of gasification section (2-I) and the thermal insulation layer b (219) cooling layer b (215) is arranged; Pyrolysis section (2-II) and gasification section (2-I) go to upper and lower layout and directly communicate, and pyrolysis section (2-II) is at epimere, and gasification section (2-I) is at hypomere; The internal diameter of vapourizing furnace is 1.25m, and interior outage degree is 9m; Gasification section (2-I) furnace wall is designed to the back taper solid of revolution; On the back taper solid of revolution furnace wall of gasification section (2-I), 20 plasma torchs are set; Plasma torch is multilayer ring-type layout, and spout points to the axle center, and 7 water vapor spray guns are set between the interval of plasma torch; On the furnace wall on pyrolysis section (2-II) top, there is pyrolysis gas outlet (204) to pick out; On the furnace wall of gasification section (2-I) and pyrolysis section (2-II) combining site, there is syngas outlet (217) to pick out, on the furnace wall of the position, middle and lower part of gasification section (2-I), has pyrolysis gas to melt down import (208) respectively and melt down import (209) access with the charcoal ash; The opening for feed of fixed-bed gasification furnace (2) is arranged on the furnace roof; The top of pyrolysis section (2-II) has pyrolysis gas outlet (204) to pick out; In the ingress of pyrolysis gas outlet (204) louver is set and keeps off grey device (203); Pyrolysis gas outlet (204) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber outlet (814) of heat exchanger (8) is melted down import (208) through the pyrolysis gas that pipe connecting a (28) is connected to fixed-bed gasification furnace gasification section (2-I); Syngas outlet (217) on the furnace wall of gasification section (2-I) top is connected to the synthetic gas import (603) of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down import (209) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fixed-bed gasification furnace gasification section (2-I); The syngas outlet (601) of gas-solid separator (6) is connected to the synthetic gas import (802) of heat exchanger (8) through pipe connecting d (7); The syngas outlet (805) of heat exchanger (8) is connected to the synthetic gas import (1001) of waste heat boiler through pipe connecting e (9), and the syngas outlet (1301) of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14).Coal cinder enters into fixed-bed gasification furnace (2) through carbonic acid gas sealing gland feeding unit; Carbonic acid gas sealing gland feeding unit is made up of coal hopper (3005), closed scraper plate coal conveyor (30); Wherein, Carbonic acid gas sealing gland (3008) is arranged in the coal hopper (3005), and going up in addition in coal hopper (3005), carbonic acid gas replenishes mouthful (3006), carbonic acid gas detects mouthful (3007); Closed scraper plate coal conveyor (30) is made up of driving wheel (3002), follow-up pulley, material loading scraper plate (3001), dividing plate (3010), backhaul scraper plate (3011) and closed shell (3009); Opening for feed (3003) top of closed scraper plate coal conveyor (30); Scraper conveyor discharge port (3012) endways; Opening for feed (3003) weighing apparatus of the discharge port of coal hopper (3005) and closed scraper plate coal conveyor (30) connects, and scraper conveyor discharge port (3012) connects with opening for feed (201) weighing apparatus of fixed-bed gasification furnace (2).The structure of the structure of the materials for wall of vapourizing furnace, gasification section body of wall internal cooling layer and mode of connection, heat exchanger (8) and the mode of connection of mode of connection, plasma torch and water vapor spray gun are all identical with the 1st embodiment, no longer describe here.
The above embodiments 2 are when operation; Coal crusher to particle diameter is 20～30mm, enters in the vapourizing furnace through the top of carbonic acid gas sealing gland feeding unit from fixed-bed gasification furnace (2), fills the space of gasification section (2-I) and pyrolysis section (2-II); The required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coal in the stove; Part in the gaseous state thing that the interior gasification of gasification section (2-I) generates is as heat-carrying gas, and under the graviational interaction of fluidized wind machine (4), the heat-carrying gas in the stove is moved to pyrolysis section (2-II) through the space between coal cinder by gasification section (2-I) outside stove; Be delivered to pyrolysis section (2-II) to the heat of gasification section (2-I); The coal cinder of stove is gone in heating, and makes the coal cinder effusion water vapor and the pyrolysis gas of pyrolysis section, becomes coke behind coal cinder effusion water vapor and the pyrolysis gas and gets into gasification section (2-I); In plasma torch, be heated to water vapor more than 4000 ℃, decompose generation H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the coke, carry out chemical reaction with coke and generate CO, H 2, CO 2, CH 4Synthetic gas, and emit heat energy, subsequently CO 2Carry out reduction reaction with coke again and generate CO, spray into gasification section (2-I) to water vapor through the water vapor spray gun simultaneously, having water vapor to participate under the situation of reaction CH 4With water vapor or CO 2Reaction generates CO and H 2Synthetic gas, form slag behind the coke gasification and enter slag bath through slag notch, water seal; The water vapor, the pyrolysis gas that generate at pyrolysis section (2-II) mix with heat-carrying gas; Pyrolysis gas outlet (204) by pyrolysis section (2-II) top is drawn outside the stove; Get into the sub-air chamber (803) of heat exchanger (8) then through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5); Enter into collection chamber (815) through heat exchanger tube (810) again, make the intensification of through heat exchanger tube (810) time, being heated indirectly of heat-carrying mixed gas, come out by collection chamber outlet (814) then; In pipe connecting a (28) returned the gasification section (2-I) of fixed-bed gasification furnace (2), water vapor wherein and coke carried out chemical reaction and generate CO and H 2Synthetic gas, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Synthetic gas; Generate in the vapourizing furnace with CO and H 2For the synthetic gas of staple is drawn by the syngas outlet (217) on gasification section (2-I) top; Get into gas-solid separator (6) through pipe connecting b (29) and separate, isolated charcoal ash returns the gasification section (2-I) of fixed-bed gasification furnace (2) and carries out gasification process, and isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8); Give the heat-carrying mixed gas in the heat exchanger tube (810) the heat indirect exchange; Draw by heat exchange chamber (809) then, after the cooling of waste heat boiler recovery heat, carry out dedusting, desulfurizing and purifying processing again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.Present embodiment is in operation; Working pressure in the fixed-bed gasification furnace (2) is controlled between negative pressure 30Pa～malleation 500Pa; Service temperature in the gasification section (2-I) is controlled between 1000～1500 ℃; Service temperature in the pyrolysis section (2-II) is controlled between 300～1000 ℃, and the residence time of coal cinder in stove is greater than 45min; In stove, import the water vapor vaporized chemical of coal cinder weight 60～85% simultaneously; Be sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, 45% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II).Working pressure and service temperature are controlled through the output flow of adjusting synthetic gas and the electric power of plasma torch and the input of water vapor in the stove.
The gasification rate of the foregoing description 1 and embodiment 2 almost reaches 100%, and when selecting for use III class hard coal to be gasified raw material, the parameter of coal is: V y=7.85%, C y=65.65%, H y=2.64%, O y=3.19%, N y=0.99%, S y=0.51%, A y=19.02%, W y=8%, Q y Dw=24426kj/kg; In the synthetic gas of coming out of the stove after the gasification per ton: CO=50535mol, H 2=66469mol, CO 2=3189mol, CH 4=984mol, N 2=354mol.The synthetic gas of coming out of the stove is again through after cooling, dedusting, desulfurizing and purifying and the conversion process; As the virgin gas of producing methyl alcohol; Coal per ton can be produced the 1100kg methanol product; When the carbonic acid gas in the waste gas was not recycled, the carbonic acid gas of discharging was about 633kg, produced methyl alcohol per ton and reduced coal consumption about 40%, reducing emission of carbon dioxide about 45% than routine techniques.

Claims (10)

1. the method for a gasifying coal by using plasma comprises the fluidized-bed gasification technology, and the workflow design that it is characterized in that fluidized-bed gasification furnace (1) is three sections mode of operation; Present, in, following layout; Epimere is suspension preheating section (a 1-IV), and the stage casing is turbulent flow pyrolysis section (a 1-III), hypomere bubbling gasification section (1-II); Plasma torch is arranged on bubbling gasification section (1-II); With the working gas of water vapor as plasma torch, make water vapor more than plasma torch internal heating to 4000 ℃, decompose and generate H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the coke of bubbling gasification section (1-II), react as follows:
C(s)+4H *=CH 4+75.6kj
C(s)+2O *=CO 2+566kj
C(s)+2H 2 *=CH 4+75.6kj
2C(s)+2HO *=2CO+H 2-131.2kj
C(s)+O2 *=CO 2+566kj
The activity chemistry thing of water molecules and coke carry out chemical reaction and generate CO, H 2, CO 2, CH 4, and emit heat energy, subsequently CO 2Carry out reduction reaction with coke again and generate CO, the water vapor spray gun is set simultaneously, having water vapor to participate under the situation of reaction CH in bubbling gasification section (1-II) 4With water vapor or CO 2Reaction generates CO and H 2, the required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coke in the stove; Fluidized wind is taken from the gasification resultant in the fluidized-bed gasification furnace (1); Outside stove under the graviational interaction of fluidized wind machine (4); Fluidized wind is operation from bottom to top in stove; The bubbling gasification section of flowing through (1-II), turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV) are drawn outside the stove by the top outlet of suspension preheating section (1-IV) again, return the air compartment (1-I) in the fluidized-bed gasification furnace (1) through fluidisation airduct a (3) and fluidisation blower fan (4) then; Get into bubbling gasification section (1-II) through the blast cap (110) on the air distribution plate (109) again; Carry out circular flow, fluidized wind is the double as perolene also, the thermal energy transfer of bubbling gasification section (1-II) to turbulent flow pyrolysis section (1-III) and suspension preheating section (1-IV); Coal dust or coal water slurry spray into the suspension preheating section (1-IV) in the fluidized-bed gasification furnace (1) by spray gun; Carry out preheating and evaporate water vapor in suspension preheating section (1-IV), the coal grain falls into turbulent flow pyrolysis section (1-III) with the free setting mode then, rolls up and down at turbulent flow pyrolysis section (1-III) and is heated; Become coke granule behind the effusion pyrolysis gas and fall into bubbling gasification section (1-II); In bubbling gasification section (1-II), coke granule moves up and down with the bubbling fluidization mode, and the activity chemistry thing that sprays with plasma gun carries out chemical reaction; Reach with water vapor and carry out chemical reaction, generate CO and H 2Synthetic gas, become molten slag until being gasified totally and enter the water seal slag bath; The pyrolysis gas that generates at turbulent flow pyrolysis section (1-III) mixes with fluidized wind; Enter into suspension preheating section (1-IV); The water vapor that generates with suspension preheating section (1-IV) mixes again; Draw outside the stove through the outlet of the top of suspension preheating section (1-IV); Air compartment (1-I) and the blast cap (110) on the air distribution plate (109) through fluidisation airduct a (3) and fluidisation blower fan (4), fluidized-bed gasification furnace (1) enter in the bubbling gasification section (1-II), and water vapor wherein and coke carry out chemical reaction and generate CO and H 2, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Generate in the fluidized-bed gasification furnace (1) with CO and H 2For the syngas mixture of staple is come out by the syngas outlet on bubbling gasification section (1-II) top; Getting into gas-solid separator (6) separates; Isolated carbon granule returns the bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) and carries out gasification process, and isolated synthetic gas carries out dedusting, desulfurizing and purifying processing after reclaiming the heat cooling through waste heat boiler again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.
2. the method for a kind of gasifying coal by using plasma according to claim 1; It is characterized in that the working pressure in the fluidized-bed gasification furnace (1) is controlled between 0～5kPa; The service temperature of suspension preheating section (1-IV) is controlled between 270～330 ℃; The service temperature of turbulent flow pyrolysis section (1-III) is controlled between 750～850 ℃, and the service temperature of bubbling gasification section (1-II) is controlled between 1100～1200 ℃; Fluidized wind in the fluidized-bed gasification furnace (1) is designed to three sections wind speed; The mean wind speed of bubbling gasification section (1-II) is 1～2.5m/s; The wind speed of turbulent flow pyrolysis section (1-III) is 3～5m/s; The wind speed of suspension preheating section (1-IV) is 1～2m/s, and the residence time of gasified raw material in stove is greater than 15min.
3. the method for a kind of gasifying coal by using plasma according to claim 1; It is characterized in that when with coal dust during as gasified raw material; The particle diameter of coal dust is 30～150 μ m; The water vapor vaporized chemical of input coal dust weight 60～85% in stove simultaneously is sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, and 45% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II); When with coal water slurry during as gasified raw material; The ratio of moisture is 30～40% in the coal water slurry; The particle diameter of coal is less than 50 μ m; In stove, add the water vapor vaporized chemical of coal water slurry total amount 45% simultaneously, wherein 80% of water vapor vaporized chemical addition through being sprayed on the coke in the bubbling gasification section (1-II) after the plasma torch decomposition activation, and 20% of water vapor vaporized chemical addition is directly imported in the bubbling gasification section (1-II).
4. the method for a kind of gasifying coal by using plasma according to claim 1; It is characterized in that being provided with heat exchanger (8) and gas-solid separator (6) in the periphery of vapourizing furnace; Fluidized wind in the fluidized-bed gasification furnace (1) is taken pyrolysis G&W steam and is drawn outside the stove by the top of suspension preheating section (1-IV); Get into the sub-air chamber (803) of heat exchanger (8) then through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5); Enter into collection chamber (815) through heat exchanger tube (810) again; Make the fluidized wind intensification of through heat exchanger tube (810) time, being heated indirectly, come out by collection chamber outlet (814) then, the air compartment (1-I) through pipe connecting a (28), fluidized-bed gasification furnace (1) returns bubbling gasification section (1-II); The synthetic gas that generates in the fluidized-bed gasification furnace (1) is come out by the syngas outlet on bubbling gasification section (1-II) top; Getting into gas-solid separator (6) through pipe connecting b (29) separates; Isolated charcoal ash returns the bubbling gasification section (1-II) of fluidized-bed gasification furnace (1) and carries out gasification process; Isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8), gives the fluidized wind in the heat exchanger tube (810) the heat indirect exchange, is come out by heat exchange chamber (809) then; After the cooling of waste heat boiler recovery heat, send into subsequent handling and handle.
5. equipment of realizing the said method of claim 1; It is characterized in that fluidized-bed gasification furnace (1) is made up of suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I); Suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) and air compartment (1-I) are in same solid of revolution furnace wall; Present between suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III) and the bubbling gasification section (1-II), in, following layout and directly communicating; Suspension preheating section (1-IV) is at epimere, and turbulent flow pyrolysis section (1-III) is in the stage casing, and bubbling gasification section (1-II) is at hypomere; Below the bubbling gasification section (1-II) air compartment (1-I); Between bubbling gasification section (1-II) and the air compartment (1-I) air distribution plate (109) is arranged, the slag notch of bubbling gasification section (1-II) is arranged on the outer periphery of air distribution plate (109), and slag notch is layout in the form of a ring; Plasma torch and water vapor spray gun are installed on the furnace wall of bubbling gasification section (1-II); On the furnace wall on the top of suspension preheating section (1-IV), there is fluidized wind outlet (103) to pick out, on the furnace wall at 1/2 following position of suspension preheating section (1-IV), pulverized coal gun or coal water slurry spray gun (123) access arranged; On the furnace wall on bubbling gasification section (1-II) top, there is syngas outlet to pick out; On the furnace wall of air compartment (1-I), there is fluidized wind import (108) to insert.
6. a kind of equipment according to claim 5; The bubbling gasification section (1-II) that it is characterized in that fluidized-bed gasification furnace (1) adopts heart-shaped design; Plasma torch on the furnace wall of bubbling gasification section (1-II) is the multilayer layout, and every layer of ring-type is provided with many plasma torchs, and the spout of plasma torch points to the stove inner axes; The water vapor spray gun is set between the interval of plasma torch, and the water vapor spray gun is at least one; The solid of revolution furnace wall of fluidized-bed gasification furnace (1) is made up of fire-resistant furnace wall a (120), thermal insulation layer a (121) and Steel Sheel a (122), wherein between the fire-resistant furnace wall a (120) of bubbling gasification section (1-II) and the thermal insulation layer a (121) cooling layer a (115) is arranged; The internal diameter of suspension preheating section (1-IV) is 1.5 times of turbulent flow pyrolysis section (1-III); The mean inside diameter of bubbling gasification section (1-II) is 1.3 times of turbulent flow pyrolysis section (1-III) diameter, and the aspect ratio of suspension preheating section (1-IV), turbulent flow pyrolysis section (1-III), bubbling gasification section (1-II) is 1.5:1.3:1; The slag notch of bubbling gasification section (1-II) is communicated to air compartment (1-I) through slagging channel (111), is water seal (107) below the air compartment (1-I); Peripherals at fluidized-bed gasification furnace (1) also has fluidisation blower fan (4), heat exchanger (8), gas-solid separator (6) and waste heat boiler (10); Fluidized wind on suspension preheating section (1-IV) top furnace wall outlet (103) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber of heat exchanger (8) exports (814) are connected to fluidized-bed gasification furnace air compartment (1-I) through pipe connecting a (28) fluidized wind import (108); Syngas outlet on bubbling gasification section (1-II) the top furnace wall is connected to the synthetic gas import of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down interface (104) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fluidized-bed gasification furnace bubbling gasification section (1-II); The syngas outlet of gas-solid separator (6) is connected to the synthetic gas import of heat exchanger (8) through pipe connecting d (7); The syngas outlet of heat exchanger (8) is connected to the synthetic gas import of waste heat boiler (10) through pipe connecting e (9), and the syngas outlet of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14).
7. the method for a gasifying coal by using plasma comprises the fixed bed gasification technology, and the workflow that it is characterized in that fixed-bed gasification furnace (2) is two sections mode of operation; Go to upper and lower layout, epimere is pyrolysis section (a 2-II), and hypomere is gasification section (a 2-I); Plasma torch is arranged on gasification section (2-I); With the working gas of water vapor as plasma torch, water vapor is heated in plasma torch more than 4000 ℃, decomposes to generate H *, O *, H 2 *, HO *, O 2 *Behind the activity chemistry thing, inject directly on the coke of gasification section (2-I), react as follows:
C(s)+4H *=CH 4+75.6kj
C(s)+2O *=CO 2+566kj
C(s)+2H 2 *=CH 4+75.6kj
2C(s)+2HO *=2CO+H 2-131.2kj
C(s)+O 2 *=CO 2+566kj
The activity chemistry thing of water molecules and coke carry out chemical reaction and generate CO, H 2, CO 2, CH 4, and emit heat energy, subsequently CO 2Carry out reduction reaction with coke again and generate CO, the water vapor spray gun is set simultaneously, having water vapor to participate under the situation of reaction CH in gasification section (2-I) 4With water vapor or CO 2Reaction generates CO and H 2, the required heat of gasification reaction is provided by the thermopositive reaction and the high-temperature plasma of activity chemistry thing and coke in the stove; Coal cinder is got in the fixed-bed gasification furnace (2) by the opening for feed of furnace roof; Fill the space of gasification section (2-I) and pyrolysis section (2-II); Part in the gaseous state thing that the interior gasification of gasification section (2-I) generates is as heat-carrying gas, and under the graviational interaction of fluidized wind machine (4), the heat-carrying gas in the stove is moved to pyrolysis section (2-II) by gasification section (2-I) outside stove; Be delivered to pyrolysis section (2-II) to the heat of gasification section (2-I); The coal cinder of stove is gone in heating, makes coal cinder effusion water vapor and pyrolysis gas into stove, becomes coke behind coal cinder effusion water vapor and the pyrolysis gas and gets into gasification section (2-I); Water vapor, pyrolysis gas that pyrolysis section (2-II) generates mix with heat-carrying gas; Pyrolysis gas outlet (204) by pyrolysis section (2-II) top is drawn outside the stove; Get into the sub-air chamber (803) of heat exchanger (8) then through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5); Enter into collection chamber (815) through heat exchanger tube (810) again; Make the intensification of through heat exchanger tube (810) time, being heated indirectly of heat-carrying mixed gas; Come out by collection chamber outlet (814) then, in pipe connecting a (28) returned the gasification section (2-I) of fixed-bed gasification furnace (2), water vapor wherein and coke carried out chemical reaction and generate CO and H 2, coal smoke, gaseous state tar, C in the pyrolysis gas mH n, CH 4React generation CO and H with water vapor 2Form slag behind the coke gasification in the gasification section (2-I) and enter slag bath through slag notch, water seal; Generate in the fixed-bed gasification furnace (2) with CO and H 2For the synthetic gas of staple is drawn by the syngas outlet on gasification section (2-I) top; Get into gas-solid separator (6) through pipe connecting b (29) and separate, isolated charcoal ash returns the gasification section (2-I) of fixed-bed gasification furnace (2) and carries out gasification process, and isolated synthetic gas enters into the heat exchange chamber (809) of heat exchanger (8); Give the heat-carrying mixed gas in the heat exchanger tube (810) the heat indirect exchange; Draw by heat exchange chamber (809) then, after the cooling of waste heat boiler recovery heat, carry out dedusting, desulfurizing and purifying processing again; Send into the synthetic gas basin; As the virgin gas utilization of producing methyl alcohol or dme, or as the utilization of hydrogen feedstock gas, or as the town gas utilization.
8. the method for a kind of gasifying coal by using plasma according to claim 7; It is characterized in that the working pressure in the fixed-bed gasification furnace (2) is controlled between negative pressure 30Pa～malleation 500Pa; Service temperature in the gasification section (2-I) is controlled between 1000～1500 ℃; Service temperature in the pyrolysis section (2-II) is controlled between 300～1000 ℃, and the coal cinder particle diameter that is input in the stove is 20～30mm, and the residence time of coal cinder in stove is greater than 45min; In stove, import the water vapor vaporized chemical of coal cinder weight 60～85% simultaneously; Be sprayed on the coke in the bubbling gasification section (1-II) after 55% of water vapor vaporized chemical decomposes activation through plasma torch, 45% of water vapor vaporized chemical is directly imported in the bubbling gasification section (1-II).
9. equipment of realizing the said method of claim 7; It is characterized in that fixed-bed gasification furnace (2) is made up of pyrolysis section (2-II) and gasification section (2-I); Pyrolysis section (2-II) and gasification section (2-I) are in same solid of revolution furnace wall, and pyrolysis section (2-II) and gasification section (2-I) go to upper and lower layout and directly communicate, and pyrolysis section (2-II) is at epimere; Gasification section (2-I) is provided with plasma torch and water vapor spray gun at hypomere on the furnace wall of gasification section (2-I); On the furnace wall on pyrolysis section (2-II) top, there is pyrolysis gas outlet (204) to pick out; On the furnace wall of gasification section (2-I) and pyrolysis section (2-II) combining site, there is syngas outlet to pick out, on the furnace wall of gasification section (2-I), has pyrolysis gas to melt down import (208) respectively and melt down import (209) access with the charcoal ash; The opening for feed of fixed-bed gasification furnace (2) is arranged on the furnace roof; Pyrolysis gas outlet (204) on the pyrolysis section (2-II) is connected to sub-air chamber's import (801) of heat exchanger (8) through fluidisation airduct a (3), fluidisation blower fan (4) and fluidisation airduct b (5), and the collection chamber outlet (814) of heat exchanger (8) is melted down import (208) through the pyrolysis gas that pipe connecting a (28) is connected to fixed-bed gasification furnace gasification section (2-I); Syngas outlet on gasification section (2-I) the top furnace wall is connected to the synthetic gas import of gas-solid separator (6) through pipe connecting b (29), and the charcoal ash outlet (602) of gas-solid separator (6) is melted down import (209) through the charcoal ash that pipe connecting c (27) and the grey transfer lime of charcoal (22) are connected to fixed-bed gasification furnace gasification section (2-I); The syngas outlet of gas-solid separator (6) is connected to the synthetic gas import of heat exchanger (8) through pipe connecting d (7); The syngas outlet of heat exchanger (8) is connected to the synthetic gas import of waste heat boiler through pipe connecting e (9), and the syngas outlet of waste heat boiler (10) is connected to follow-up equipment through synthetic gas transfer lime (14).
10. a kind of equipment according to claim 9; The solid of revolution furnace wall that it is characterized in that fixed-bed gasification furnace (2) is made up of fire-resistant furnace wall b (218), thermal insulation layer b (219) and Steel Sheel b (220), wherein between the fire-resistant furnace wall b (218) of gasification section (2-I) and the thermal insulation layer b (219) cooling layer b (215) is arranged; Gasification section (2-I) furnace wall is designed to the back taper solid of revolution; On the back taper solid of revolution furnace wall of gasification section (2-I), many plasma torchs are set; Plasma torch is multilayer ring-type layout; Spout points to the axle center, and the water vapor spray gun is set between the interval of plasma torch, and the water vapor spray gun is at least one.
CN2010101186828A 2010-02-06 2010-02-06 Method and equipment for gasifying coal by using plasma Expired - Fee Related CN101781584B (en)

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CN102134513B (en) * 2010-11-29 2013-08-07 衢州昀睿工业设计有限公司 Device for producing hydrogen from water through pyrolysis by adopting plasma and coal gasification co-production of gas
CN103194269B (en) * 2010-12-22 2014-01-29 衢州昀睿工业设计有限公司 Plasma gasification furnace for disposing garbage biomass
CN102559272B (en) * 2011-12-29 2014-05-14 武汉凯迪工程技术研究总院有限公司 Microwave plasma biomass entrained flow gasifier and process
CN103113923A (en) * 2013-02-21 2013-05-22 山东润银生物化工股份有限公司 Four-segment spray coal oxygen-enriched gasification method
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CN108373934A (en) * 2018-05-18 2018-08-07 华北电力大学（保定） Multiple types Biomass Gasification in Circulating Fluidized Bed reactor and its gasification process
CN108676580B (en) * 2018-06-28 2023-09-12 内蒙古科技大学 High Wen Jiaohu type double-fixed bed gasification furnace and process method thereof

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