CN1318796C - Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer - Google Patents
Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer Download PDFInfo
- Publication number
- CN1318796C CN1318796C CNB2004100707663A CN200410070766A CN1318796C CN 1318796 C CN1318796 C CN 1318796C CN B2004100707663 A CNB2004100707663 A CN B2004100707663A CN 200410070766 A CN200410070766 A CN 200410070766A CN 1318796 C CN1318796 C CN 1318796C
- Authority
- CN
- China
- Prior art keywords
- steam
- combustion chamber
- returning charge
- coal
- charge section
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 15
- 239000012530 fluid Substances 0.000 title claims abstract description 14
- 239000006200 vaporizer Substances 0.000 title claims description 59
- 238000000197 pyrolysis Methods 0.000 title claims description 56
- 238000002485 combustion reaction Methods 0.000 claims abstract description 63
- 239000003245 coal Substances 0.000 claims abstract description 48
- 238000002156 mixing Methods 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 18
- 239000003034 coal gas Substances 0.000 claims description 15
- 238000009826 distribution Methods 0.000 claims description 14
- 238000002309 gasification Methods 0.000 claims description 9
- 238000011049 filling Methods 0.000 claims description 6
- 239000000463 material Substances 0.000 abstract description 16
- 238000000354 decomposition reaction Methods 0.000 abstract 5
- 239000000571 coke Substances 0.000 abstract 4
- 230000008016 vaporization Effects 0.000 abstract 3
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 238000005243 fluidization Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The present invention relates to a method for producing both gas and steam and a boiler of a circulating fluid bed, and the boiler of a circulating fluid bed comprises a fluid bed combustion chamber, a cyclone separator, a hot ash distributer, a heat decomposition vaporizing chamber and a differential bed recycled material device, wherein coal is conveyed to the combustion chamber of the boiler of the circulating fluid bed by a feeding machine and is combusted in the combustion chamber, and flue gas generated by combustion enters a heat exchanger through the cyclone separator and generates the steam. Circulating ash in the flue gas is collected by the cyclone separator, a part of the circulating ash directly returns the combustion chamber, the other part of the circulating ash enters the movable bed heat decomposition vaporizing chamber and provides heat quantity for the heat decomposition of the coal, the gas is generated, semi coke generated by the heat decomposition returns the combustion chamber, and the semi coke is combusted in the combustion chamber. The circulating ash is divided into two parts by the hot ash distributer using the steam as fluid medium, a part of the circulating ash directly returns the combustion chamber, the other part of the circulating ash and the coal enter the movable bed heat decomposition vaporizing chamber, the circulating ash and the coal are decomposed in heat after the circulating ash and the coal are mixed by a fixed mixing device, the generated semi coke returns the combustion chamber through the differential bed recycled material device using the steam as the fluid medium, and the semi coke is combusted in the combustion chamber. The boiler of a circulating fluid bed has the characteristics that the boiler of a circulating fluid bed can be independently operated as a steam boiler, and both the gas and the steam can be produced; the generated quantity of the gas and components are stable, and heat value is high; regulation is.
Description
Technical field
The present invention relates to the CFBB of a kind of coal gas-steam combined production method and band pyrolysis vaporizer.
Technical background
Existing coal-burning boiler and gasification furnace can only be single production steam and coal gas, and existing coal gas-steam joint production boiler often only guarantees stable Gas Production.For fluid bed coal gas-steam co-producing equipment, vaporizer commonly used has two kinds of forms, i.e. moving bed gasification chamber and bubbling bed vaporizer.In the moving bed gasification chamber, semicoke returns the combustion chamber and often adopts the gravity flow mode, the time of staying of the uncontrollable material of this mode in vaporizer, has influenced the conversion ratio of carbon; And the material returning device on the regular circulation fluidized-bed combustion boiler is not suitable for herein yet, because the particle diameter of semicoke is much larger than boiler circulating ash particle diameter, 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 impurity content in the coal gas.Simultaneously, existing fluid 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 92100912 provides a kind of production method and device of dry distillation gas, and its device mainly comprises CFBB, fluidized bed dryer, dry distiller and material pneumatic conveying system.Circulating ash partly or entirely enters dry distiller, and by the ash amount that the control of ash amount adjustment doors enters dry distiller, this mechanical type ash amount adjustment doors is at high temperature worked, and cost, life-span and reliability are all very undesirable.Circulating ash and coal are sent into two inlets on the dry distiller respectively, are difficult for mixing in dry distiller, have reduced efficiency of carbon con version.The semicoke and the circulating ash of discharging from the destructive distillation chamber are sent burner hearth by forced air back to pneumatic conveying mode, and required air quantity is big, and the speed height easily causes the burning of semicoke in carrier pipe, and bigger to the carrier pipe wearing and tearing.
Summary of the invention
The purpose of this invention is to provide a kind of coal gas-steam combined production method, this method is: coal is sent into the burning of burning in circulating fluid bed boiler chamber through batcher, the flue gas that burning produces enters heat exchanger through cyclone separator and produces steam, circulating ash in the flue gas is captured by cyclone separator, a part is directly returned the combustion chamber, another part enters the moving bed pyrolysis vaporizer and provides heat for the pyrolysis of coal, produces coal gas, and pyrogenous origin semicoke returns combustion chambers burn; Circulating ash is by with the hot grey distributor separated into two parts of steam as fluidizing agent, a part is directly returned the combustion chamber, another part enters the moving bed pyrolysis vaporizer with coal, pyrolysis after the blending of fixed blending device, the semicoke of generation is by returning combustion chambers burn with steam as the differential bed material-returning device of fluidizing agent.
Another object of the present invention provides the CFBB of a kind of Tape movement bed pyrolysis vaporizer, this CFBB can be stable simultaneously production steam and coal gas, and can regulate the intensity of gasification and steam flow respectively, and can control the time of staying of coal in pyrolysis vaporizer, improve coal utilizaton rate, also can suppress the generation of tar by control vaporizer temperature.
Technical scheme of the present invention is as follows:
Coal gas-steam combined production method provided by the invention, this method is: coal is sent into the burning of burning in circulating fluid bed boiler chamber through batcher, the flue gas that burning produces enters heat exchanger through cyclone separator and produces steam, circulating ash in the flue gas is captured by cyclone separator, a part is directly returned the combustion chamber, another part enters the moving bed pyrolysis vaporizer and provides heat for the pyrolysis of coal, produces coal gas, and pyrogenous origin semicoke returns combustion chambers burn; It is characterized in that: circulating ash is by with the hot grey distributor separated into two parts of steam as fluidizing agent, a part is directly returned the combustion chamber, another part enters the moving bed pyrolysis vaporizer with coal, pyrolysis after the blending of fixed blending device, the semicoke of generation is by returning combustion chambers burn with steam as the differential bed material-returning device of fluidizing agent.
The CFBB of being with pyrolysis vaporizer provided by the invention comprises:
One fluidized bed combustion chamber 1; Described fluidized bed combustion chamber 1 is regular circulation fluidized-bed combustion boiler combustion chamber, and its underpart locular wall is provided with stokehold coal feeding hole 11 and desulfurizing agent adds inlet 12, and the bottom of fluidized bed combustion chamber 1 is provided with fluidization air inlet 13, is furnished with wall-cooling surface in the combustion chamber;
One cyclone separator 2; Described cyclone separator 2 inlets are connected with fluidized bed combustion chamber 1 top;
One hot grey distributor 3; The grey distributor 3 of described heat comprises feed zone 31 that is arranged on top and the returning charge section 32 and 33 that is positioned at feed zone 31 both sides; Feed zone 31, returning charge section 32 and returning charge section 33 bottoms are connected, and its arranged beneath has the air distribution plate 34 of band blast cap; The air compartment 35,36,37 and 38 of air distribution plate 34 arranged beneath word orders; Its left side air compartment 35 be positioned at left side returning charge section 32 under, right side air compartment 38 be positioned at right side returning charge section 33 under, the air compartment 36 and 37 in the middle of being positioned at be positioned at feed zone 31 under; Described feed zone 31 is connected with the bottom of cyclone separator 2; Described left side returning charge section 32 is communicated with fluidized bed combustion chamber 1 bottom;
One pyrolysis vaporizer 4; Described pyrolysis vaporizer 4 tops are cylinder barrel shaped, and the bottom is inverted round platform tubular, and its top is provided with coal filling hole 39; Its top is provided with inlet pipeline section 41 and the gas outlet tube 43 that internal diameter is d1, and described inlet pipeline section 41 is connected with returning charge section 33; One fixed blending device 42 is set under the inlet pipeline section 41 of pyrolysis vaporizer 4 inside, and this fixed blending device 42 is a cone;
One is positioned at the differential bed material-returning device 5 of the below of pyrolysis vaporizer 4; Described differential bed material-returning device 5 comprises: be positioned at feed zone 51 and returning charge section 52 that the bottom on its top is connected, the below of described feed zone 51 and returning charge section 52 is provided with the air distribution plate 53 of band blast cap, and air distribution plate 53 belows are provided with the air compartment 54 and 55 that in-line is arranged; Described left side air compartment 54 is positioned under the feed zone 51, and described right side air compartment 55 is positioned under the returning charge section 52; Described returning charge section 52 is connected with 1 bottom, combustion chamber; Described feed zone 51 is connected with the lower end outlet of pyrolysis vaporizer 4.
One heat exchanger 6, described heat exchanger 6 links to each other with cyclone separator 2 exhanst gas outlets, hot water from combustion chamber 1 wall-cooling surface enters heat exchanger 6, by flue gas heating from cyclone separator 2, produce steam, part steam is as the fluidizing agent of grey distributor 3 of heat and differential bed material-returning device 5.
The conical surface of described fixed blending device 42 is provided with guiding gutter.The cone bottom surface diameter d 2 of described fixed blending device 42 is 2d1, cone height h1=(2～5) d2.
Boiler provided by the present invention the fluidized bed combustion chamber that has except that the regular circulation fluidized-bed combustion boiler, cyclone separator, the material returning device, also has moving bed pyrolysis vaporizer and differential bed material-returning device; Material returning device also is different from routine, is the grey distributor of heat, except that having circulating ash is sent back to the effect of combustion chamber, also has the effect that circulating ash with the ratio of the circulating ash that enters the moving bed pyrolysis vaporizer of combustion chamber are directly returned in adjusting concurrently.Fluidized bed combustion chamber top is communicated with cyclone separator; The grey distributor of heat is arranged in the separator bottom, is communicated with moving bed pyrolysis vaporizer top and bottom, combustion chamber respectively; Differential bed material-returning device links to each other bottom, moving bed gasification chamber with the bottom, combustion chamber.Boiler also is provided with coal feeding hole on the inlet pipeline section above the pyrolysis vaporizer except that the coal supply of stokehold, coal and circulating ash promptly began blending before entering pyrolysis vaporizer, but not the two enters pyrolysis vaporizer respectively, thereby has striven for more reaction time.
In service, regulate hot grey distributor and distribute to the heat ash amount of pyrolysis vaporizer, the returning charge amount of differential bed material-returning device, and the coal-supplying amount of pyrolysis vaporizer's top coal feeding hole, can make pyrolysis vaporizer stable produce coal gas by specified productive rate; Heat ash amount and coal-supplying amount that gas yield mainly leans on hot grey distributor to distribute to pyrolysis vaporizer are controlled, and strengthening hot ash amount and coal-supplying amount can increase gas yield, otherwise then reduces gas yield.Simultaneously, regulate the stokehold coal-supplying amount, hot grey distributor is dispensed to the heat ash amount of directly returning burner hearth, and the returning charge amount of differential bed material-returning device, can make boiler stable produce steam by specified productive rate; The steam productive rate is mainly controlled this method of employing by stokehold coal-supplying amount and returning charge ash amount, and boiler can be stable simultaneously provides steam and coal gas.
Differential bed material-returning device of the present invention can be sent the high-temp solid material of particle diameter in 0-8 millimeter scope back to combustion chamber by the pneumatic control mode from pyrolysis vaporizer, and can be regulated the solid matter streams rate.Its fluidizing agent is a steam, feeds material-returning device by feed zone and returning charge section bottom, regulates two sections fluidization steam vapor amount, causes the fluidizing velocity of material poor, thereby forms the pressure reduction from feed zone to the returning charge section, promotes material and returns burner hearth.What be different from conventional material returning device is that the steam that the feed zone bottom feeds only enters from the one side of something near the returning charge section.In addition, the feed zone lower side also can feed compressed air as cross air blasting.
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 commercial Application or generating, and solid impurity and tar content are very low in the coal gas, can be used for Chemical Manufacture; 2. can be applicable to newly-built recirculating fluidized bed coal gas-steam co-producing stove, perhaps the reconstruction of regular circulation fluidized-bed combustion boiler is coal gas-steam co-producing stove; 3. the coal gas amount and the stable components of Chan Shenging, the calorific value of gas height; 4. the Gas Production flow process only need be supplied steam, and system's operation is regulated flexible; 5. the semicoke that produces in the gasification furnace is sent into the combustion chamber after-flame, can effectively improve the coal utilization rate; 6. by desulfurizing agents such as adding lime stones in the combustion chamber, can realize efficient simple honest and clean desulfurization in the stove, reduce environmental pollution.
Description of drawings
Fig. 1 is the flow chart of the embodiment of the invention;
Fig. 2 is the hot grey distributor component diagram of the embodiment of the invention;
Fig. 3 is the differential bed material-returning device component diagram of the embodiment of the invention.
Fluidized bed combustion chamber 1 stokehold coal feeding hole 11 desulfurizing agents add inlet 12
Fluidization air 13 cyclone separators, the 2 hot grey distributors 3 that enter the mouth
Feed zone 31 returning charge sections 32,33 air distribution plates 34
Air compartment 35,36,37,38 pyrolysis vaporizer, 4 coal filling holes 39
Inlet pipeline section 41 inlet pipeline sections 41 inner diameter d 1 gas outlet tube 43
Fixed blending device 42 differential bed material-returning devices 5 feed zones 51
Returning charge section 52 air distribution plates 53 air compartments 54,55 heat exchangers 6
The cone bottom surface diameter d 2 of fixed blending device 42
The cone height h1 of fixed blending device 42
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples:
As shown in Figure 1, the CFBB of being with pyrolysis vaporizer provided by the invention comprises fluidized bed combustion chamber 1, cyclone separator 2, hot grey distributor 3, pyrolysis vaporizer 4, differential bed material-returning device 5 and subsidiary conduit;
Described fluidized bed combustion chamber 1 is regular circulation fluidized-bed combustion boiler combustion chamber, and its underpart locular wall is provided with stokehold coal feeding hole 11 and desulfurizing agent adds inlet 12, and the bottom of fluidized bed combustion chamber 1 is provided with fluidization air inlet 13, is furnished with wall-cooling surface in the combustion chamber;
Described cyclone separator 2 side inlets are connected with fluidized bed combustion chamber 1 top, and top exit is communicated with heat exchanger 6;
As shown in Figure 2, the grey distributor 3 of described heat comprises feed zone 31 that is arranged on top and the returning charge section 32 and 33 that is positioned at feed zone 31 both sides; Feed zone 31, returning charge section 32 and returning charge section 33 bottoms are connected, and its arranged beneath has the air distribution plate 34 of band blast cap; The air compartment 35,36,37 and 38 of air distribution plate 34 arranged beneath word orders; Its left side air compartment 35 be positioned at left side returning charge section 32 under, right side air compartment 38 be positioned at right side returning charge section 33 under, the air compartment 36 and 37 in the middle of being positioned at be positioned at feed zone 31 under; Described feed zone 31 is connected with the bottom of cyclone separator 2; Described left side returning charge section 32 is communicated with fluidized bed combustion chamber 1 bottom;
Described pyrolysis vaporizer 4 tops are cylinder barrel shaped, and the bottom is inverted round platform tubular, and its top is provided with inlet pipeline section 41 and the gas outlet tube 43 that internal diameter is d1; Described inlet pipeline section 41 is connected with returning charge section 33, and the top is provided with coal filling hole 39; One fixed blending device 42 is set under the inlet pipeline section 41 of pyrolysis vaporizer 4 inside, and this fixed blending device 42 is a cone;
As shown in Figure 3, described differential bed material-returning device 5 is positioned at the below of pyrolysis vaporizer 4, comprise: be positioned at feed zone 51 and returning charge section 52 that the bottom on its top is connected, the below of described feed zone 51 and returning charge section 52 is provided with the air distribution plate 53 of band blast cap, and air distribution plate 53 belows are provided with the air compartment 54 and 55 that in-line is arranged; Described left side air compartment 54 is positioned under the feed zone 51, and described right side air compartment 55 is positioned under the returning charge section 52; Described returning charge section 52 is connected with 1 bottom, combustion chamber; Described feed zone 51 is connected with the lower end outlet of pyrolysis vaporizer 4.
The conical surface of described fixed blending device 42 is provided with guiding gutter.The cone bottom surface diameter d 2 of described fixed blending device 42 is 2d1, cone height h1=(2～5) d2.
During the CFBB operation of band of the present invention pyrolysis vaporizer, add coal from coal filling hole 41, enter pyrolysis vaporizer 4 with circulating ash, the fixed blending device 42 of flowing through mixes coal and high-temp circulating ash, temperature in the vaporizer 4 reaches 800-900 ℃, coal generation pyrolytic reaction generates coal gas and semicoke, is difficult for generating tar under this temperature.Coal gas is discharged from the gas exit 43 of pyrolysis vaporizer.Air compartment 54 and air compartment 55 to differential bed material-returning device 5 feed two strands of steam as fluidizing agent, entering the semicoke of differential bed material-returning device 5 and circulating ash, to produce fluidizing velocity in feed zone 51 and returning charge section 52 poor, material porosity difference in two sections flows to combustion chamber 1 from vaporizer 4 thereby produce pressure reduction promotion material.The running temperature of combustion chamber 1 maintains about 950 ℃, and semicoke burns away therein, adds 12 lime stones that the add calcining and decomposing at high temperature that enters the mouth from desulfurizing agent.The circulating ash of carrying secretly in the flue gas is captured by cyclone separator 2, falls into the feed zone 31 of hot grey distributor 3, and partial material is returned combustion chamber 1 through returning charge section 32, and another part enters vaporizer 4 through returning charge section 33, and brings a large amount of heats into, as the thermal source of pyrolytic reaction.The calcium oxide that limestone calcination generates reacts with sulfur dioxide in the boiler combustion loop, generate solid-state calcium sulfate, in vaporizer 4 with coal in the hydrogen sulfide that generates of sulphur react, generate solid-state calcium sulfide, they stably are enriched in end slag and the flying dust and discharge, and greatly reduce the sulfur content in flue gas and the coal gas.
The ratio of the fluidisation air quantity of air compartment 35, air compartment 36, air compartment 37 and air compartment 38 by changing hot grey distributor 3, can regulate circulating ash and enter the ratio of returning charge section 32 and returning charge section 33, promptly regulate circulating ash and returned combustion chamber 1 and the adjusting that enters the ratio of vaporizer 4, thereby regulated the temperature of pyrolysis vaporizer 4, the adjustment of the coal-supplying amount of cooperation coal filling hole 41 and the returning charge rate of differential bed material-returning device 5 can realize the control to gas yield.Regulate the coal-supplying amount of stokehold coal feeding hole 11 again, can realize control 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.
Differential bed material-returning device 5, feed zone 51 internal diameters are d3, returning charge section internal diameter is d4, d3=d4.Channel height between feed zone 51 and the returning charge section 52 is h2, h2=d3.The clean returning charge of returning charge section highly is h3, h3=(0.2～1) h2.Returning charge section 52 bottoms arrange that evenly blast cap feeds the steam of boiler for producing, as fluidizing agent.Blast cap is arranged near the semi-circular portion of returning charge section 52 in feed zone 51 bottoms, also feeds steam as fluidizing agent.Differential bed material-returning device 5 can be carried the solid material of 0-8 millimeter particle diameter, and can regulate the material flow rate of passing through differential bed material-returning device 5 by the steam flow of regulating air compartment 54 and air compartment 55, thereby the control time of staying of material in vaporizer 4, guarantee that the pyrolysis of coal has the enough reaction time.
Claims (5)
1, a kind of coal gas-steam combined production method, coal is sent into the burning of burning in circulating fluid bed boiler chamber through batcher, the flue gas that burning produces enters heat exchanger through cyclone separator and produces steam, circulating ash in the flue gas is captured by cyclone separator, a part is directly returned the combustion chamber, another part enters the moving bed pyrolysis vaporizer and provides heat for the pyrolysis of coal, produces coal gas, and pyrogenous origin semicoke returns combustion chambers burn; It is characterized in that: circulating ash is by with hot grey distributor (3) separated into two parts of steam as fluidizing agent, a part is directly returned combustion chamber (1), another part enters moving bed pyrolysis vaporizer (4) with coal, pyrolysis after fixed blending device (42) blending, the semicoke of generation is by returning combustion chambers burn with steam as the differential bed material-returning device (5) of fluidizing agent.
2, a kind of CFBB with pyrolysis vaporizer comprises fluidized bed combustion chamber, cyclone separator, hot grey distributor, pyrolysis vaporizer and differential bed material-returning device, it is characterized in that:
The grey distributor of described heat (3) comprises the feed zone (31) that is arranged on top and is positioned at the returning charge section (32,33) of feed zone (31) both sides; Feed zone (31), returning charge section (32) and returning charge section (33) bottom are connected, and its arranged beneath has the air distribution plate (34) of band blast cap; The air compartment (35,36,37,38) of air distribution plate (34) arranged beneath word order; Its left side air compartment (35) be positioned at left side returning charge section (32) under, right side air compartment (38) be positioned at right side returning charge section (33) under, the air compartment (36,37) in the middle of being positioned at be positioned at feed zone (31) under; Described feed zone (31) is connected with the bottom of cyclone separator (2); Described left side returning charge section (32) is communicated with fluidized bed combustion chamber (1) bottom;
Described pyrolysis vaporizer (4) top is cylinder barrel shaped, the bottom is inverted truncated cone-shaped, its top is provided with gas outlet tube (43), and it is that the inlet pipeline section (41) of d1 communicates with the returning charge section (33) of hot grey distributor (3) that its top is provided with internal diameter, and inlet pipeline section (41) is provided with coal filling hole (39); Be provided with fixed blending device (42) under the inlet pipeline section (41);
Described differential bed material-returning device (5) is positioned at the below of pyrolysis vaporizer (4), comprise: the internal diameter that the bottom is connected is the feed zone (51) of d3 and the returning charge section (52) that internal diameter is d4, the below of described feed zone (51) and returning charge section (52) is provided with the air distribution plate (53) of band blast cap, air distribution plate (53) below is provided with the air compartment (54,55) that in-line is arranged; Described left side air compartment (54) is positioned under the feed zone (51), and described right side air compartment (55) is positioned under the returning charge section (52); Described returning charge section (52) is connected with bottom, combustion chamber (1); Described feed zone (51) is connected with the lower end outlet of pyrolysis vaporizer (4).
3, by the CFBB of the described band of claim 2 pyrolysis vaporizer, it is characterized in that the indoor fixed blending device (42) of described pyrolytic gasification is a cone; The conical surface of described fixed blending device (42) is provided with guiding gutter.
4, by the CFBB of the described band of claim 2 pyrolysis vaporizer, it is characterized in that, described differential bed material-returning device (5), feed zone (51) inner diameter d 3 equates with returning charge section (52) inner diameter d 4; Channel height between described feed zone (51) and the returning charge section (52) is h2, h2=d3; The clean returning charge of described returning charge section highly is h3, h3=(0.2～1) h2; Blast cap is evenly arranged in described returning charge section (52) bottom, feeds the steam of boiler for producing, as fluidizing agent; Blast cap is arranged near the semi-circular portion of returning charge section (52) in described feed zone (51) bottom, also feeds steam as fluidizing agent.
By the CFBB of the described band of claim 3 pyrolysis vaporizer, it is characterized in that 5, the cone bottom surface diameter d 2 of described fixed blending device (42) is 2 times of inlet pipeline section (41) inner diameter d 1, cone height h1=(2～5) d2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100707663A CN1318796C (en) | 2004-07-26 | 2004-07-26 | Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100707663A CN1318796C (en) | 2004-07-26 | 2004-07-26 | Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1727750A CN1727750A (en) | 2006-02-01 |
| CN1318796C true CN1318796C (en) | 2007-05-30 |
Family
ID=35927168
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100707663A Expired - Fee Related CN1318796C (en) | 2004-07-26 | 2004-07-26 | Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1318796C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103608624A (en) * | 2011-06-22 | 2014-02-26 | 株式会社Ihi | Circulating fluidized bed-type gasification furnace and fluid medium flow rate control method |
| WO2014079283A1 (en) * | 2012-11-21 | 2014-05-30 | 中国东方电气集团有限公司 | External bed type double-fluidized bed system for preventing boiler contamination |
Families Citing this family (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101240196B (en) * | 2007-02-07 | 2011-08-17 | 中国科学院工程热物理研究所 | Fine coal pressurization dense phase transporting bed gasification method and device |
| JP5071473B2 (en) * | 2007-03-02 | 2012-11-14 | 株式会社Ｉｈｉ | Particle circulation control system in circulating fluidized bed furnace |
| CN101353582B (en) * | 2007-07-25 | 2010-12-01 | 中国科学院工程热物理研究所 | Solid heat carrier rapid pyrolysis method and apparatus |
| CN101362955B (en) * | 2007-08-08 | 2012-03-07 | 中国科学院工程热物理研究所 | Pyrolysis method and device of low speed bed |
| JP5200691B2 (en) * | 2008-06-20 | 2013-06-05 | 株式会社Ｉｈｉ | Fluidized bed gasification method and equipment |
| CN101429459B (en) * | 2008-12-24 | 2012-12-12 | 中国科学院工程热物理研究所 | Front-boiler coal drawhead method for pulverized coal fired boiler |
| DE102009032524B3 (en) * | 2009-07-10 | 2011-02-03 | Highterm Research Gmbh | Reactor for producing a product gas by allothermic gasification of carbonaceous feedstocks |
| CN102221263A (en) * | 2010-08-06 | 2011-10-19 | 湘潭互创洁净能源有限公司 | Assembled circulating fluidized bed heat carrier boiler |
| FI124422B (en) * | 2011-03-14 | 2014-08-29 | Valmet Power Oy | Method for ash treatment and ash treatment plant |
| CN102353042A (en) * | 2011-09-09 | 2012-02-15 | 北京交通大学 | Adjusting method for circulating ash quantity, separator and combustion system |
| CN102504842A (en) * | 2011-11-09 | 2012-06-20 | 浙江大学 | Three-fluidized-bed solid heat carrier coal pyrolysis, gasification and combustion cascade utilization method |
| CN102829474B (en) * | 2012-09-25 | 2016-04-06 | 中国东方电气集团有限公司 | A kind of dual bed systems preventing boiler heating surface from staiing |
| CN102829473B (en) * | 2012-09-25 | 2016-02-03 | 中国东方电气集团有限公司 | A kind of pyrolysis and combustion double bed solves the system that high sodium coal combustion stains |
| CN102944008B (en) * | 2012-11-21 | 2015-10-28 | 中国东方电气集团有限公司 | The system that a kind of double fluidized bed combustion stove prevents boiler heating surface from staiing |
| CN104109543A (en) * | 2013-04-16 | 2014-10-22 | 张晓� | Powder pyrolysis method using circulating fluidized bed technology |
| CN103725329A (en) * | 2013-12-24 | 2014-04-16 | 山东百川同创能源有限公司 | Low-tar pyrolytic device in dual bed structure and pyrolytic method |
| CN204574013U (en) * | 2015-03-18 | 2015-08-19 | 东方电气集团东方锅炉股份有限公司 | Large-size circulating fluidized bed pyrolytic gasification combined unit |
| CN105087025A (en) * | 2015-09-09 | 2015-11-25 | 中国华能集团清洁能源技术研究院有限公司 | Moving bed coal pyrolysis based polygeneration device and method |
| CN105823039B (en) * | 2016-04-21 | 2018-11-09 | 山东科院天力节能工程有限公司 | A kind of distillation system that circulating fluidized bed combustion is combined with rotary kiln pyrogenation |
| CN107270281A (en) * | 2017-07-03 | 2017-10-20 | 国丰新能源江苏有限公司 | Biomass recirculating fluidized bed boiler and its operation method |
| CN107308664B (en) * | 2017-08-11 | 2022-10-18 | 中冶焦耐(大连)工程技术有限公司 | Pneumatic circulating evaporation device and method |
| CN107502388B (en) * | 2017-09-11 | 2020-07-07 | 哈尔滨工业大学 | Two-stage low-temperature gasification device and method based on low-order fuel autocatalysis |
| CN108504388A (en) * | 2018-04-04 | 2018-09-07 | 太原锅炉集团有限公司 | A kind of low-grade fuel gasification system and its operation method |
| CN109456800B (en) * | 2018-12-12 | 2024-02-23 | 浙江工业大学 | Household garbage cascade utilization system and method based on double-bed pyrolysis |
| CN112013381B (en) * | 2020-09-01 | 2023-03-07 | 中国科学院工程热物理研究所 | Coupling double fluidized bed low-nitrogen combustion device and method |
| CN114719623B (en) * | 2022-05-18 | 2024-03-22 | 中国石油化工股份有限公司 | Heating furnace system, combustion and heat recovery method of heating furnace system |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1062751A (en) * | 1992-02-18 | 1992-07-15 | 北京水利电力经济研究所 | A kind of method and device of producing dry distillation gas |
| WO1993017958A1 (en) * | 1992-03-06 | 1993-09-16 | Commonwealth Scientific And Industrial Research Organisation | Process for producing a gaseous product |
| CN2192807Y (en) * | 1994-04-20 | 1995-03-22 | 开封锅炉厂 | Energy-saving outer circulation fluidizing bed boiler |
| CN2232040Y (en) * | 1995-11-03 | 1996-07-31 | 清华大学 | Moving-bed pyrolysis chamber gas-steam joint producing furnace |
| CN1155573A (en) * | 1996-01-26 | 1997-07-30 | 清华大学 | Process and apparatus for producing hot gas carried on cokes and vapor by fluid bed simultaneously |
| US5666801A (en) * | 1995-09-01 | 1997-09-16 | Rohrer; John W. | Combined cycle power plant with integrated CFB devolatilizer and CFB boiler |
| JPH1019206A (en) * | 1996-06-28 | 1998-01-23 | Mitsubishi Heavy Ind Ltd | Circulation amount control device |
| CN1377938A (en) * | 2001-03-30 | 2002-11-06 | 中国科学院化工冶金研究所 | Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel |
-
2004
- 2004-07-26 CN CNB2004100707663A patent/CN1318796C/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1062751A (en) * | 1992-02-18 | 1992-07-15 | 北京水利电力经济研究所 | A kind of method and device of producing dry distillation gas |
| WO1993017958A1 (en) * | 1992-03-06 | 1993-09-16 | Commonwealth Scientific And Industrial Research Organisation | Process for producing a gaseous product |
| CN2192807Y (en) * | 1994-04-20 | 1995-03-22 | 开封锅炉厂 | Energy-saving outer circulation fluidizing bed boiler |
| US5666801A (en) * | 1995-09-01 | 1997-09-16 | Rohrer; John W. | Combined cycle power plant with integrated CFB devolatilizer and CFB boiler |
| CN2232040Y (en) * | 1995-11-03 | 1996-07-31 | 清华大学 | Moving-bed pyrolysis chamber gas-steam joint producing furnace |
| CN1155573A (en) * | 1996-01-26 | 1997-07-30 | 清华大学 | Process and apparatus for producing hot gas carried on cokes and vapor by fluid bed simultaneously |
| JPH1019206A (en) * | 1996-06-28 | 1998-01-23 | Mitsubishi Heavy Ind Ltd | Circulation amount control device |
| CN1377938A (en) * | 2001-03-30 | 2002-11-06 | 中国科学院化工冶金研究所 | Four coproduction process and equipment for circular fluiding carbon-hydrogen solid fuel |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103608624A (en) * | 2011-06-22 | 2014-02-26 | 株式会社Ihi | Circulating fluidized bed-type gasification furnace and fluid medium flow rate control method |
| CN103608624B (en) * | 2011-06-22 | 2016-02-24 | 株式会社Ihi | Circulate the flow control methods of laminar gasification furnace and flow media |
| US9528053B2 (en) | 2011-06-22 | 2016-12-27 | Ihi Corporation | Circulating fluidized bed-type gasification furnace and fluid medium flow rate control method |
| WO2014079283A1 (en) * | 2012-11-21 | 2014-05-30 | 中国东方电气集团有限公司 | External bed type double-fluidized bed system for preventing boiler contamination |
| US9784445B2 (en) | 2012-11-21 | 2017-10-10 | Dongfang Electric Corporation | External bed type double-fluidized bed system for preventing boiler contamination |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1727750A (en) | 2006-02-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1318796C (en) | Method for producing both gas and steam, and boiler of circulating fluid bed with pyrolysis vaporizer | |
| CN100390254C (en) | Coal gas-steam combined production method and apparatus of double-circulation fluidized bed | |
| CN101353582B (en) | Solid heat carrier rapid pyrolysis method and apparatus | |
| CN108753368B (en) | Circulating fluidized bed coal gasification system and method | |
| CN103555370B (en) | Carbonaceous organic material gasification process and vapourizing furnace | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN101220298B (en) | Thermal decomposition gasification method and device of circulating fluidized bed | |
| CZ20014156A3 (en) | Device for gasification of carbonaceous charge material | |
| CN107043641B (en) | Coal gasification method and device of circulating fluidized bed with fine ash return | |
| AU2007353259A1 (en) | A coal circulating fluidized bed coal gas generating furnace system | |
| CN104629809B (en) | The system that high heating value biomass gasified gas are produced with oxygen-enriched combustion boiler high-temperature flue gas | |
| CN102911740A (en) | Two-section gasifying device of entrained-flow bed and gasifying method of two-section gasifying device | |
| CN101362955B (en) | Pyrolysis method and device of low speed bed | |
| CN111763535A (en) | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification | |
| CN106753580B (en) | Self-loopa fluidized-bed gasification furnace in a kind of stove | |
| CN100458282C (en) | Method for burning petroleum coke or gasified remained coke, and inner mixed type combustion equipment | |
| CN103242907A (en) | High-pressure multistage fluidized bed reactor | |
| US8257453B2 (en) | Method and device for gasifying gasification fuel | |
| CN208649244U (en) | A kind of circulation fluidized bed coal gasifying system | |
| CN100543116C (en) | The oxygen deprivation fluidized bed combustion downdraft gasification process and the device that prepare no tar products gas | |
| UA79669C2 (en) | Method and unit for production of low temperature coke | |
| CN102124084B (en) | Fluidized-bed gasification method and facility therefor | |
| CN116143425B (en) | Central burner type lime kiln | |
| CN102492477A (en) | Hierarchical oxygen supply and controllable flame coal water slurry entrained bed combined nozzle | |
| CN205295251U (en) | Two sections pyrolysis gasification system of solid waste |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070530 Termination date: 20180726 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |