CN1754945A - Double-circulating fluid bed coal gas-steam combined production method and device - Google Patents
Double-circulating fluid bed coal gas-steam combined production method and device Download PDFInfo
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- CN1754945A CN1754945A CN200410081018.5A CN200410081018A CN1754945A CN 1754945 A CN1754945 A CN 1754945A CN 200410081018 A CN200410081018 A CN 200410081018A CN 1754945 A CN1754945 A CN 1754945A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
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Abstract
Gas and steam co-production that the present invention relates to and coproduction stove, fuel burns in the combustion chamber, the flue gas that produces enters the heat exchanger heats water generates steam through cyclonic separator, directly returned the combustion chamber by the circulating ash part that cyclonic separator captures, another part enters vaporizer, the reaction of fuel generation pyrolytic gasification produces coal gas, and reacted Jiao/semicoke returns combustion chambers burn; The coproduction stove and accessory has double-circulating fluid bed loop, it is the burning loop of circulating fluidized bed combustor, smoke separator, material returning device composition, gasification loop with circulating fluidized bed vaporizer, coal gas separator, material returning device composition, two loops are by hot grey divider and the coupling of bed material material returning device, make burning and gasification both interrelated, relatively independent again, thus realization steam and coal gas are stablized output, independent regulation; Its operation scheme is flexible, except that as the coproduction stove operation, but independent operating also.Except that coal, this method also can be used for pyrolysis or gasification carbonaceous refuse or alternative fuel.
Description
Technical field
The present invention relates to a kind of double-circulating fluid bed coal gas-steam combined production method and double-circulating fluid bed coal gas-steam co-producing device.
Technical background
Existing coal firing boiler and vapourizing furnace can only produce steam or coal gas singlely, and existing coal gas-steam joint production boiler often only guarantees the stable of gas production, can not guarantee the stable of production of steam simultaneously.For fluidized-bed coal gas-steam co-producing equipment, there are two kinds of forms gasification chamber commonly used: moving-bed gasification chamber and bubbling bed coal-gasification chamber.In moving-bed gasification chamber, circulating ash is difficult for mixing with coal, has restricted the raising of efficiency of carbon conversion; In addition, the semicoke in the vaporizer returns the combustion chamber and often adopts from stream mode, the residence time of the uncontrollable material of this mode in vaporizer, has influenced the transformation efficiency of carbon; And the material returning device on the regular circulation fluidized-bed combustion boiler is not suitable for the moving-bed gasification chamber yet, because the particle diameter of semicoke is much larger than the circulating ash particle diameter of regular circulation fluidized-bed combustion boiler, flowability also differs widely.Bubbling bed vaporizer can be controlled the returning charge of material easily, but because fluidizing gas velocity is higher than moving-bed, the particle of being carried secretly by elutriation increases greatly, has increased flying dust and has contained carbon loss, has also increased the foreign matter content in the coal gas.Simultaneously, existing fluidized-bed coal gas-steam co-producing technology, the mode that adopts circulating ash all to enter vaporizer makes burning and gasification be difficult to control respectively coal gas and steam productive rate independent regulation difficulty more.
Chinese invention patent 92100503.2 provides a kind of gas-steam combine producing process and device, adopts fluidized bed coal gasifier, and coal enters burner hearth by vapourizing furnace, and the reaction times in vapourizing furnace is shorter; And the circulating ash that burning produces all enters vapourizing furnace, can only guarantee gas yield, can not guarantee the supply and the adjusting of steam and coal gas simultaneously; Directly outer confession of the coal gas that produces, carry-over loss is bigger, has reduced efficiency of carbon conversion.
Chinese invention patent 92100912.7 provides a kind of method and device of producing dry distillation gas, is made of circular fluid bed, fluidized bed dryer, dry distiller and material pneumatic conveying system etc.The recycle stock part is directly got back to burner hearth, and part enters dry distiller; But dry distiller moves in the moving-bed mode, and circulating ash and coal add respectively, is difficult for mixing, and gasification efficiency is not high; The coal that adds dry distiller enters burner hearth by dry distiller, and the reaction times in dry distiller is shorter; Material distributes by the mechanical valve realization in addition, and reliability is low.
China's utility model patent 01230778.5 provides a kind of fluidized bed pulverized coal gasification producer gas generator, have double-fluidized-bed, have smoke separator behind the fluid-bed combustion furnace, have coal gas separator behind the fluidized bed coal steam stove, but all materials all will flow through gas furnace, coal gas separator, roasting kiln and smoke separator successively, thereby it burns and gasification does not possess independent circulation loop, but the series circulation in the burning loop and the loop of gasifying not is proper double-circulating fluid bed; Cycle gasification reaction institute heat requirement all is to bring gas furnace into by the thermal material that burning produces; This stove is only supplied coal gas, can not produce steam simultaneously.In addition, less through the coal grain yardstick after the gasification, part coal grain will discharge with flue gas or coal gas without after-flame, has reduced efficiency of carbon conversion; All materials all are alternately by gas furnace and roasting kiln, this operation scheme requires coal particle more carefully could once take out of, and regular circulation fluidized-bed (material particular diameter is between 0-10mm) has very big difference, can't bring into play the repeatedly circulation of circulating fluidized bed and the effect of score of firings like this, and make system regulate difficulty, gasification efficiency and efficiency of combustion certainly will be lower.The conveying of cold and hot material is finished by mechanical worm conveyor in addition, has reduced reliability of system operation.
Summary of the invention
One of purpose of the present invention provides a kind of gas and steam co-production.Fuel burns in the combustion chamber, the flue gas that produces enters the heat exchanger heats water generates steam through cyclonic separator, directly returned the combustion chamber by the circulating ash part that cyclonic separator captures, another part enters vaporizer, fuel generation pyrolysis and part coal gasification reaction produce coal gas, and reacted Jiao/semicoke returns combustion chambers burn; Characteristics are: material is in the combustion chamber and the combustion cycle loop formed of smoke separator, material returning device, the gasification circulation loop of forming with vaporizer and coal gas separator, material returning device, two circulation loop internal recycling, also between two circulation loops, circulate simultaneously, but but also independent operating of two circulation loop cooperations; The heat that burning produces is used for heated feed water or/and pyrolytic gasification reaction institute heat requirement is provided; The high-temp circulating ash that pyrolytic gasification reaction institute heat requirement produces from burning, the perhaps afterburning of fuel and coal gas; Fuel and circulating ash even blend, in vapourizing furnace the residence time long, institute's producing coal pneumatolytic divides the stable caloric value height; System regulates flexibly, the utilization ratio height of fuel; The fuel that this method can be used for pyrolysis or gasification not only comprises coal, also comprises carbonaceous refuse and alternative fuel (as rubber, plastics and the sludge-drying etc. of biomass, fragmentation).
The present invention also aims to propose a kind of double-circulating fluid bed coal gas-steam co-producing device, this combination preparing device has double-circulating fluid bed loop, it is the burning loop of circulating fluidized bed combustor, smoke separator, material returning device composition, gasification loop with circulating fluidized bed vaporizer, coal gas separator, material returning device composition, wherein material returning device that join the combustion chamber is for delivering to circulating ash the hot grey divider of combustion chamber and vaporizer, and material returning device that vaporizer is joined is for returning the circulating ash foldback the conventional material returning device of vaporizer; Expect that by the bed of bottom, hot grey gentleization of divider chamber material returning device is communicated with between two circulation loops, be coupled, make burning and gasification promptly interrelated, separate again, thereby realize the stable output and the independent regulation of steam and coal gas.
Technical scheme of the present invention is as follows:
Double-circulating fluid bed coal gas-steam combined production method provided by the invention, fuel burns in the combustion chamber, the flue gas that produces enters the heat exchanger heats water generates steam through cyclonic separator, directly returned the combustion chamber by the circulating ash part that cyclonic separator captures, another part enters vaporizer, fuel generation pyrolysis and partial gasification reaction produce coal gas, and reacted semicoke returns combustion chambers burn; It is characterized in that: material is in the combustion chamber and the combustion cycle loop formed of smoke separator, material returning device, and the gasification circulation loop formed of vaporizer and coal gas separator, material returning device, two circulation loop internal recycling; Also between two circulation loops, circulate simultaneously, the circulating ash that burning produces is distributed by the hot grey divider of pneumatic control, a part is directly returned burner hearth, another part enters vaporizer, and Jiao/semicoke in the vaporizer and circulating ash are returned to the combustion chamber by the bed material material returning device of the pneumatic control of vaporizer bottom; But but also independent operating of two circulation loop cooperations; The fluidizing medium of vaporizer is air, steam and coal gas, perhaps is the gas mixture of air and steam, perhaps is the gas mixture of air and coal gas; The heat that burning produces is used for heated feed water or/and pyrolytic gasification reaction institute heat requirement is provided; The high-temp circulating ash that pyrolytic gasification reaction institute heat requirement mainly comes auto-combustion to produce if the vaporizer temperature is not high enough, can adopt the afterburning of fuel and coal gas.
The fuel that this method can be used for pyrolysis or gasification not only comprises coal, also comprises carbonaceous refuse and alternative fuel (as rubber, plastics and the sludge-drying etc. of biomass, fragmentation).
The afterburning of described fuel and coal gas in vaporizer, in the hot grey divider or gas exit carry out.The working temperature of described combustion chamber is 800-1000 ℃, and the working temperature of pyrolysis vaporizer is 700-950 ℃.
Double-circulating fluid bed coal gas provided by the invention-steam co-producing device comprises:
One combustion chamber 1; Described fluidised bed combustion chamber 1 bottom locular wall is provided with front-furnace feeding mouth 11, sweetening agent adds inlet 14, circulating ash returning charge mouth 12 and semicoke returning charge mouth 13,1 bottom, combustion chamber is provided with fluidization air inlet 15 and end slag discharge outlet, is furnished with wall-cooling surface in the combustion chamber 1 or makes adiabatic wall;
The one cigarette wind separator 2 that is connected with 1 top, combustion chamber; The top smoke outlet tube 21 of this cigarette wind separator 2 is communicated with the heat exchanger 8 of carrying vapour outlet;
One hot grey divider 5; The grey divider 5 of described heat comprises feed zone 51 that is arranged on top and the returning charge section 52 and 53 that is positioned at feed zone 51 both sides; The bottom of feed zone 51 and returning charge section 52,53 is connected, and its arranged beneath has the air distribution plate 54 of band blast cap; The air compartment 55,56,57 and 58 of air distribution plate 54 arranged beneath word orders; Its left side air compartment 55 be positioned at left side returning charge section 52 under, right side air compartment 58 be positioned at right side returning charge section 53 under, be positioned at intermediary air compartment 56 and 57 be positioned at feed zone 51 under; Described feed zone 51 is connected with cigarette wind separator 2 bottoms; Described left side returning charge section 52 is connected with the circulating ash returning charge mouth 12 of 1 bottom, combustion chamber;
One pyrolysis vaporizer 3; Described pyrolysis vaporizer 3 bottom locular walls are provided with material inlet 31, combustion cycle ash inlet 32 and gasification circulating ash returning charge mouth 33, and the bottom is provided with gasification agent inlet 34; Described combustion cycle ash inlet 32 is connected with the returning charge section 53 of hot grey divider 5;
A material material returning device 6; This material material returning device 6 is positioned at vaporizer 3 bottoms and communicates with vaporizer 3 bottoms, comprise the outlet section 62 that is arranged on the following inlet section of pyrolysis vaporizer's air distribution plate 61 and is positioned at inlet section 61 opposite sides, inlet section 61 is communicated with outlet section 62 bottoms, its arranged beneath has the air distribution plate 63 of band blast cap, air distribution plate 63 arranged beneath have the air compartment 64,65 and 66 of word order, right side air compartment 64 is positioned under the inlet section 61, left side air compartment 65 is positioned under the outlet section 62, and described outlet section 62 is connected with combustion chamber 1 bottom semicoke returning charge mouth 13; It is characterized in that, also comprise:
One coal gas separator 4; These coal gas separator 4 inlets are connected with vaporizer 3 tops, and the top is provided with gas outlet tube 41;
One material returning device 7; This material returning device 7 is positioned at coal gas separator 4 belows, and its inlet is connected with coal gas separator 4, and outlet is connected with the gasification circulating ash returning charge mouth 33 of vaporizer 3 bottoms.
Co-production of the present invention and combination preparing device, can stably produce steam and coal gas simultaneously, can regulate pyrolytic gasification parameter and steam parameter respectively, and the residence time of may command material in pyrolysis vaporizer, improve gasification efficiency, also can suppress the generation of macromole (as tar) by the temperature of control pyrolysis vaporizer; Can realize high-efficiency desulfurization in the stove by to sweetening agents such as the indoor adding Wingdales of pyrolytic gasification, reduce H in the coal gas significantly
2The concentration of S.
Co-production of the present invention and combination preparing device, have two Circulating Fluidized Bed loops, a burning loop and a gasification loop, two loops are by hot grey divider and the coupling of bed material material returning device, make burning and pyrolytic gasification process not only interrelated but also relatively independent, thereby realize steam and stable output of coal gas and independent regulation.
Co-production of the present invention and combination preparing device, operation scheme is flexible, except that the coproduction mode is moved, also can be used as two independent device operations, instant heating ash divider goes back to the whole foldbacks of circulating ash to the combustion chamber, the bed material material returning device of pyrolysis vaporizer bottom not the foldback material to the combustion chamber; The combustion chamber still produces steam, and pyrolysis vaporizer moves in partial combustion partial gasification mode, produces coal gas.
Co-production of the present invention and combination preparing device, the combustion chamber is moved with conventional combustion system, and pyrolysis vaporizer can three kinds of modes move:
A) pyrolysis of fuel.Pyrolysis vaporizer feeds coal gas or CO
2, N
2As fluidizing medium, fuel absorbs the heat that circulating ash that hot grey divider sends into is brought into, and pyrolytic reaction takes place, and produces pyrolysis coal gas Deng rare gas element;
B) gasification of fuel.The mixture of vaporizer bubbling air, water vapor, oxygen or these gases is as fluidizing medium, and fuel is the generating gasification reaction in vaporizer, produces coal gas;
C) gasification of fuel and afterburning.When the indoor temperature of pyrolytic gasification was on the low side, fuel easily produced larger molecular organicses such as tar in the pyrolytic gasification process; Can promote temperature this moment by the mode of burn a part of fuel or coal gas, decomposes these larger molecular organicses.Afterburning can carry out three kinds of positions: 1. carry out afterburning in vaporizer, bubbling air or steam and Air mixing gas are as the fluidizing medium of vaporizer, and heat is emitted in part of fuel and gas-fired, and the generating gasification that acts as a fuel is reacted replenishing of institute's heat requirement; 2. in the returning charge section that the grey divider of heat is communicated with vaporizer, carry out afterburning, bubbling air burns away the fuel in the circulating ash as the fluidizing medium of this returning charge section, improves the temperature of circulating ash, thereby bring more heats in vaporizer, and improve the temperature of vaporizer; 3. carry out afterburning at the vaporizer gas exit, provide air and part gas-fired heat release, improve gas temperature at gas exit.
Characteristics of the present invention are: 1. can also can realize coal gas-steam co-producing separately as the steam boiler operation, steam can be used for industrial application or generating, and the content of larger molecular organics in the coal gas (as tar) is very low; 2. can be applicable to newly-built circulating fluidized bed coal gas-steam co-producing stove, also can be used for the reconstruction of regular circulation fluidized-bed combustion boiler is coal gas-steam co-producing stove; 3. pyrolytic gasification stove moves in the circulating fluidized bed mode, fuel and circulating ash even blend, and long at the gasification residing time in furnace, gasification reaction is complete, and the coal gas of generation is output after cyclonic separator purifies, stable components, caloric power of gas height; 3. pyrolytic gasification stove can pyrolysis or gasification of coal, and carbonaceous refuse and alternative fuel (as biomass, broken rubber, plastics and sludge-drying etc.); 4. gas production process flow operation mode is various, and system's operation is regulated flexible; 5. the semicoke that produces in the vapourizing furnace is sent into the combustion chamber after-flame, can effectively improve fuel availability; 6. by to sweetening agents such as the indoor adding Wingdales of pyrolytic gasification, can realize efficient simple honest and clean desulfurization in the stove, reduce environmental pollution.
Description of drawings
Fig. 1 is the schema of the embodiment of the invention;
Fig. 2 is the hot grey divider component diagram of the embodiment of the invention;
Fig. 3 is the bed material material returning device component diagram of the embodiment of the invention.
Semicoke returning charge mouth 13 sweetening agents add inlet 14 fluidization airs inlet 15
Gasification agent inlet 34 coal gas separators 4 gas outlet tubes 41
The grey divider 5 feed zones 51 returning charge sections 52,53 of heat
55,56,57,58 material of air distribution plate 54 air compartments material returning device 6
Embodiment
The invention will be further described below in conjunction with drawings and Examples:
As shown in Figure 1, the invention provides double-circulating fluid bed coal gas-steam co-producing stove, comprise combustion chamber 1, cyclonic separator 2, hot grey divider 5, vaporizer 3, cyclonic separator 4, material returning device 7, bed material material returning device 6 and subsidiary conduit etc.;
Described combustion chamber 1 bottom locular wall is provided with front-furnace feeding mouth 11, sweetening agent adds inlet 14, circulating ash returning charge mouth 12 and semicoke returning charge mouth 13, and the bottom of combustion chamber 1 is provided with fluidization air inlet 15, and combustion chamber wall is wall-cooling surface or adiabatic wall;
Described cyclonic separator 2 inlets are connected with 1 top, combustion chamber, and the exhanst gas outlet 21 at top is communicated with heat exchanger 6;
Described vaporizer 3 bottom locular walls are provided with material inlet 31, combustion cycle ash inlet 32 and gasification circulating ash returning charge mouth 33, and the bottom is provided with gasification agent inlet 34;
Described cyclonic separator 4 inlets are connected with vaporizer 3 tops, and the top is provided with gas outlet tube 41;
As shown in Figure 2, the grey divider 5 of described heat comprises feed zone 51 that is arranged on top and the returning charge section 52 and 53 that is positioned at feed zone 31 both sides; Feed zone 51, returning charge section 52 and returning charge section 53 bottoms are connected, and its arranged beneath has the air distribution plate 54 of band blast cap; The air compartment 55,56,57 and 58 of air distribution plate 54 arranged beneath word orders; Its left side air compartment 55 be positioned at left side returning charge section 52 under, right side air compartment 58 be positioned at right side returning charge section 53 under, be positioned at intermediary air compartment 56 and 57 be positioned at feed zone 51 under; Described feed zone 51 is connected with the bottom of cyclonic separator 2; Described left side returning charge section 52 is communicated with 1 bottom, combustion chamber; Described right side returning charge section 53 is communicated with vaporizer 3 bottoms;
Described material returning device 7 inlets are connected with coal gas separator 4, and outlet is connected with the gasification circulating ash returning charge mouth 33 of vaporizer 3 bottoms;
As shown in Figure 3, described bed material material returning device 6 comprises entrance 61 that is arranged on below the vaporizer air distribution plate and the outlet section 62 that is communicated with combustion chamber 1 bottom semicoke returning charge mouth 13; Inlet section 61 is communicated with outlet section 62 bottoms, its arranged beneath has the air distribution plate 63 of band blast cap, air distribution plate arranged beneath air compartment 64,65 and 66, right side air compartment 64 is positioned under the inlet section 61, left side air compartment 65 is positioned under the outlet section 62, and middle air compartment 66 is under the bottom connected component between inlet section 61 and the outlet section 62;
Described heat exchanger 8 links to each other with the smoke outlet tube 21 of smoke separator 2, from the hot water of combustion chamber 1 wall-cooling surface, or the feedwater that directly enters heat exchanger 8, by flue gas heating, produce steam from smoke separator 2.
When double-circulating fluid bed coal gas of the present invention-steam co-producing stove moves, fuel fluidized bed combustion in combustion chamber 1 from 11 addings of front-furnace feeding mouth, combustion chamber 1 temperature is controlled at about 950 ℃, flue gas flow is through smoke separator 2, circulating ash is captured, flue gas is through smoke outlet tube 21 heat exchanger 8 of flowing through, and heating produces steam from the hot water or the feedwater of combustion chamber 1 wall-cooling surface; About about the 930 ℃ circulating ash of temperature enters hot grey divider 5, a part is directly returned the combustion chamber, another part enters vaporizer 4, with the fuel that adds from vaporizer material inlet 31 by vaporized chemical fluidisation and thorough mixing, temperature in the vaporizer 4 is controlled in about 850 ℃ the scope that is difficult for generation tar, the reaction of generation pyrolytic gasification, generate coal gas, the coal gas coal gas separator 4 of flowing through, Jiao/semicoke and circulating ash are captured, send vaporizer 3 back to through material returning device 7, coal gas is through gas outlet tube 41 outputs; Jiao/semicoke in the vaporizer 3 is sent combustion chamber 1 back to by bed material material returning device 6 and is burnt away; Add the Wingdale calcining and decomposing generation at high temperature calcium oxide that inlet 12 adds from sweetening agent, in the burning loop, react and generate solid-state calcium sulfate with sulfurous gas, in vaporizer 4 with fuel in the hydrogen sulfide that generates of sulphur react and generate solid-state sulfurated lime, they stably are enriched in end slag and the flying dust and discharge, and greatly reduce the sulphur content in flue gas and the coal gas.
Bed material material returning device 6 is the returning charge valve of a pneumatic control, its inlet section is a moving-bed, outlet section is the bubbling bed, by regulating the fluidisation air quantity of air compartment 64,65 and 66, can control material flow rate, thereby realize control Jiao/semicoke amount of going back to the combustion chamber from the vaporizer foldback by this material material returning device.
The ratio of the fluidisation air quantity of air compartment 55, air compartment 56, air compartment 57 and air compartment 58 by changing hot grey divider 5, can regulate circulating ash and enter the ratio of returning charge section 52 and returning charge section 53, promptly regulate circulating ash and returned combustion chamber 1 and the adjusting that enters the ratio of vaporizer 3, thereby regulated the temperature of vaporizer 3, cooperate the feeding coal of material inlet 31 and the adjustment that bed is expected the returning charge rate of material returning device 6, can realize control gas yield.The feeding coal of re-adjustment front-furnace feeding mouth 11 can be realized the control to the steam productive rate.Thereby realized the separately control of burning and gasification, guaranteed that coal gas and steam can be simultaneously by specified productive rate productions.
When steam demand is bigger, the coal gas demand hour can be regulated the fluidisation air quantity of hot grey divider, makes circulating ash mainly return the combustion chamber, the less vaporizer of even not sending into; If circulating ash is brought shortage of heat into to satisfy the needs of pyrolytic gasification reaction in the vaporizer, the vaporizer temperature is on the low side, in the time of can't maintaining in the temperature range that is difficult for generation tar, can be from vaporizer bottom bubbling air, utilize the part of fuel heat release of in vaporizer, burning, satisfy the needs of remaining fuel pyrolytic gasification reaction; Perhaps burn part coal gas, improve gas temperature and decompose tar in the vaporizer outlet.
Claims (5)
1, a kind of double-circulating fluid bed coal gas-steam combined production method, fuel burns in the combustion chamber, the flue gas that produces enters the heat exchanger heats water generates steam through cyclonic separator, directly returned the combustion chamber by the circulating ash part that cyclonic separator captures, another part enters vaporizer, the reaction of fuel generation pyrolytic gasification produces coal gas, and reacted Jiao/semicoke returns combustion chambers burn; It is characterized in that: material is in the combustion chamber and the combustion cycle loop formed of smoke separator, material returning device, and the gasification circulation loop formed of vaporizer and coal gas separator, material returning device, two circulation loop internal recycling; Also between two circulation loops, circulate simultaneously, the circulating ash that burning produces is distributed by the hot grey divider of pneumatic control, a part is directly returned burner hearth, another part enters vaporizer, and Jiao/semicoke in the vaporizer and circulating ash are returned to the combustion chamber by the bed material material returning device of the pneumatic control of vaporizer bottom; But but also independent operating of two circulation loop cooperations; The fluidizing medium of vaporizer is air, steam and coal gas, perhaps is the gas mixture of air and steam, perhaps is the gas mixture of air and coal gas; The heat that burning produces is used for heated feed water or/and pyrolytic gasification reaction institute heat requirement is provided; The high-temp circulating ash that pyrolytic gasification reaction institute heat requirement mainly comes auto-combustion to produce, the perhaps afterburning of fuel and coal gas.
2, by the described double-circulating fluid bed coal gas-steam combined production method of claim 1, it is characterized in that described fuel is coal, carbonaceous refuse or alternative fuel; Described carbonaceous refuse and alternative fuel are rubber, plastics or the sludge-drying of biomass, fragmentation.
3, by the described double-circulating fluid bed coal gas-steam combined production method of claim 1, it is characterized in that, the afterburning of described fuel and coal gas in vaporizer, in the hot grey divider or gas exit carry out.
4, by the described double-circulating fluid bed coal gas-steam combined production method of claim 1, it is characterized in that the working temperature of described combustion chamber (1) is 800-1000 ℃, the working temperature of pyrolysis vaporizer (2) is 700-950 ℃.
5, a kind of double-circulating fluid bed coal gas-steam co-producing device comprises:
One combustion chamber (1); Described fluidised bed combustion chamber (1) bottom locular wall is provided with front-furnace feeding mouth (11), sweetening agent adds inlet (14), circulating ash returning charge mouth (12) and semicoke returning charge mouth (13), bottom, combustion chamber (1) is provided with fluidization air inlet (15) and end slag discharge outlet, is furnished with wall-cooling surface or makes adiabatic wall in combustion chamber (1);
The one cigarette wind separator (2) that is connected with top, combustion chamber (1); The top smoke outlet tube (21) of this cigarette wind separator (2) is communicated with the heat exchanger (8) of carrying vapour outlet;
One hot grey divider (5); The grey divider of described heat (5) comprises the feed zone (51) that is arranged on top and is positioned at returning charge section (52) and (53) of feed zone (51) both sides; Feed zone (51) and returning charge section 52,53) the bottom be connected, its arranged beneath have the band blast cap air distribution plate (54); The air compartment (55,56,57 and 58) of air distribution plate (54) arranged beneath word order; Its left side air compartment (55) be positioned at the left side returning charge section (52) under, right side air compartment (58) be positioned at right side returning charge section (53) under, be positioned at intermediary air compartment (56) and (57) be positioned at feed zone (51) under; Described feed zone (51) is connected with cigarette wind separator (2) bottom; Described left side returning charge section (52) is connected with the circulating ash returning charge mouth (12) of bottom, combustion chamber (1);
One pyrolysis vaporizer (3); Described pyrolysis vaporizer (3) bottom locular wall is provided with material inlet (31), combustion cycle ash inlet (32) and gasification circulating ash returning charge mouth (33), and the bottom is provided with gasification agent inlet (34); Described combustion cycle ash inlet (32) is connected with the returning charge section (53) of hot grey divider (5);
A material material returning device (6); This bed material material returning device (6) is positioned at vaporizer (3) bottom and communicates with vaporizer (3) bottom, comprise the outlet section (62) that is arranged on the following inlet section (61) of pyrolysis vaporizer's air distribution plate and is positioned at inlet section (61) opposite side, inlet section (61) is communicated with outlet section (62) bottom, its arranged beneath has the air distribution plate (63) of band blast cap, air distribution plate (63) arranged beneath has the air compartment (64) of word order, (65) and (66), right side air compartment (64) is positioned under the inlet section (61), left side air compartment (65) is positioned under the outlet section (62), and described outlet section (62) is connected with combustion chamber (1) bottom semicoke returning charge mouth (13); It is characterized in that, also comprise:
One coal gas separator (4); This coal gas separator (4) inlet is connected with vaporizer (3) top, and the top is provided with gas outlet tube (41);
One material returning device (7); This material returning device (7) is positioned at coal gas separator (4) below, and its inlet is connected with coal gas separator (4), and outlet is connected with the gasification circulating ash returning charge mouth (33) of vaporizer (3) bottom.
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| CNB2004100810185A CN100390254C (en) | 2004-09-30 | 2004-09-30 | Coal gas-steam combined production method and apparatus of double-circulation fluidized bed |
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| CNB2004100810185A CN100390254C (en) | 2004-09-30 | 2004-09-30 | Coal gas-steam combined production method and apparatus of double-circulation fluidized bed |
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| CN103045275A (en) * | 2011-10-17 | 2013-04-17 | 中国科学院工程热物理研究所 | Self-heating pyrolysis method |
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Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2219429Y (en) * | 1994-10-08 | 1996-02-07 | 浙江大学 | Square exhausting-down hot-exchange separator |
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