CN103742899B - A kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique - Google Patents
A kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique Download PDFInfo
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- CN103742899B CN103742899B CN201410030446.9A CN201410030446A CN103742899B CN 103742899 B CN103742899 B CN 103742899B CN 201410030446 A CN201410030446 A CN 201410030446A CN 103742899 B CN103742899 B CN 103742899B
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 239000001301 oxygen Substances 0.000 title claims abstract description 54
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 54
- 239000012530 fluid Substances 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 71
- 238000002309 gasification Methods 0.000 claims abstract description 70
- 239000003546 flue gas Substances 0.000 claims abstract description 69
- 239000000463 material Substances 0.000 claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 43
- 239000000446 fuel Substances 0.000 claims abstract description 20
- 239000000428 dust Substances 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 239000000919 ceramic Substances 0.000 claims abstract description 9
- 238000004140 cleaning Methods 0.000 claims abstract description 7
- 238000004519 manufacturing process Methods 0.000 claims abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 5
- 230000023556 desulfurization Effects 0.000 claims abstract description 5
- 239000000203 mixture Substances 0.000 claims description 26
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 239000003034 coal gas Substances 0.000 claims description 20
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 16
- 230000001276 controlling effect Effects 0.000 claims description 16
- 238000002485 combustion reaction Methods 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 9
- 239000001569 carbon dioxide Substances 0.000 claims description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 230000003134 recirculating effect Effects 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 4
- 238000000197 pyrolysis Methods 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 239000007800 oxidant agent Substances 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000004449 solid propellant Substances 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical group [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims 1
- 229910052719 titanium Inorganic materials 0.000 claims 1
- 239000010936 titanium Substances 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 239000011285 coke tar Substances 0.000 abstract description 2
- 239000003245 coal Substances 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000011269 tar Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 4
- 239000000571 coke Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000011286 gas tar Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 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
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention provides a kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme, comprise CFBC stove and circle fluidized-bed gasification furnace, CFBC stove is connected with a separator, separator and back-end ductwork, two-way material controlling device connects, two-way material controlling device is connected with CFBC stove and circle fluidized-bed gasification furnace respectively, circle fluidized-bed gasification furnace is connected with CFBC stove by a material returning device, circle fluidized-bed gasification furnace is by No. two separators and Ceramic dust collector, gas cleaning system connects, back-end ductwork is connected with flue gas distributing valve by after the out of stock device of flue-gas dust-removing and desulfurization, the outlet of flue gas distributing valve is divided into three tunnels. the present invention also provides a kind of circulating fluid bed burning in oxygen enrichment multi-production process. the utilization ratio of system fuel provided by the invention is high, and gas yield is high, and quality of coke tar is good, and fuel and tail flue gas utilize to greatest extent, and pollutant emission is few, and cost recovery is low.
Description
Technical field
The present invention relates to a kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique, belong to coal Poly-generation skillArt field.
Background technology
China is lower to the utilization ratio of existing resource at present, especially aspect coal fired power generation or power station heat supply,Energy conversion efficiency is lower than 40%, and the utilization ratio of coal is relatively high aspect the chemical industry such as coking, oil refining,Can reach 85%～90%. Clean and effective utilizes coal resources, advances coal Poly-generation to become national strategyOne of primary study direction. Coal Poly-generation technology refers to the organic integration that is transformed, utilized technology by multiple coal,Obtain multiple clean secondary energy sources, such as electricity, liquid fuel, the change of gaseous fuel and multiple high added valueWork byproduct, realizes that coal utilization is the most efficient, minimum pollution. Evidence, power industry adopts Poly-generation systemSystem, generating efficiency can improve approximately 10%, and cost declines 30%, and simultaneously polygenerations systeme also makes chemical productsProduction cost significantly reduces.
Chinese invention patent 200610154581.X provides a kind of circulating fluidized bed heat-power-gas-tar multi-joint-production dressPut and method, by fluid-bed combustion furnace, fluidized bed dry distillation stove, high-temperature separator, material returning device and attached accordinglyGenus equipment forms, and product is mainly coal gas and tar. Fluidized bed dry distillation stove adopts recirculation coal gas or steam conductFluidizing gas, in gas retort, temperature is on the low side, and the pyrolytic reaction of coal only occurs, and most coke are in gas retortAny reaction does not occur and be just admitted to burning in combustion furnace, gas yield is very low, and part coal gas is again as streamOxidizing gases, gas yield is lower; The tar yield that fluidized bed dry distillation stove produces is higher, but tar and dust are veryDifficult separation, tar product dust burdening is difficult to greatly realize commercial Application.
Summary of the invention
It is high that the technical problem to be solved in the present invention is to provide a kind of gas yield, and tail flue gas can recycle profitWith, circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique that pollutant emission is low, really realize fuel utilizationThe most efficiently, minimum pollution.
In order to solve the problems of the technologies described above, technical scheme of the present invention is to provide a kind of circulating fluid bed burning in oxygen enrichmentPolygenerations systeme, is characterized in that: comprise CFBC stove and circle fluidized-bed gasification furnace, circular flowFluidized bed combustion stove top is connected with a separator, and No. one separator top is connected with back-end ductwork, separates for No. oneDevice bottom is connected with two-way material controlling device, two-way material controlling device respectively with CFBC stove and recirculating fluidized bed gasChange stove and connect, circle fluidized-bed gasification furnace is connected with CFBC stove by a material returning device, circular flowChange bed gasification furnace top and be connected with No. two separators, No. two separator bottoms are by No. two material returning devices and ciculation fluidizedBed gasification furnace is connected, and No. two separator top is connected with Ceramic dust collector, and Ceramic dust collector connects gas purification systemSystem, gas cleaning system is connected with air accumulator with tar pool respectively; Back-end ductwork is out of stock by flue-gas dust-removing and desulfurizationAfter device, be connected with flue gas distributing valve, the outlet of flue gas distributing valve is divided into three tunnels, the first via and flue gas oxygen mix dressPut connectedly, the second tunnel is connected with circle fluidized-bed gasification furnace, and Third Road is connected with flue gas recovery device, and air dividesBe connected with nitrogen gas recovering apparatus with flue gas oxygen mix device from device, flue gas oxygen mix device bottom and circular flowFluidized bed combustion stove is connected.
The present invention also provides a kind of circulating fluid bed burning in oxygen enrichment multi-production process, adopts above-mentioned oxygen-enriched combusting to followRing fluid bed polygenerations systeme, is characterized in that: air obtains nitrogen and oxygen after air separator separates,Nitrogen reclaims by nitrogen gas recovering apparatus, and the circulating flue gas of oxygen and oxygen-enriched combusting is in flue gas oxygen mix deviceEvenly mix, flue gas oxygen mixture is divided into two-way and sends into recirculating fluidized bed combustion as wind, a Secondary Air respectivelyBurn stove, wind, Secondary Air is as oxidant and fluidized wind and send into the fuel one in CFBC stovePlay burning, the lime-ash that burning generates is discharged at CFBC furnace bottom, and the flue gas that burning generates enters oneNumber separator, most recycle stock is separated and enters two-way material controlling device by a separator, in two-way controlUnder the regulating action of glassware, a part is returned to CFBC stove, and another part enters recirculating fluidized bed gasChange stove, the high-temperature material that enters gasification furnace provide the gasification of circle fluidized-bed gasification furnace fuel and pyrolytic reaction requiredThe heat of wanting; Control the high-temperature material amount and then the control that enter in circle fluidized-bed gasification furnace by two-way material controlling deviceThe temperature of circle fluidized-bed gasification furnace processed, reacted semicoke mixtures of materials process in circle fluidized-bed gasification furnaceMaterial returning device is sent into after-flame in CFBC stove, out untreated of circle fluidized-bed gasification furnace topCoal gas enters separator No. two, and the thin ash being separated by No. two separators returns to circular flow by No. two material returning devicesChange bed gasification furnace; The coal gas that go out on No. two separator top first passes through Ceramic dust collector, then through gas purification systemSystem in dedusting, dewater, cooling, after separating carbon dioxide, tar is reclaimed by tar pool, purify after coal gas enterAir accumulator; The flue gas that enters back-end ductwork from separator top after the out of stock device of flue-gas dust-removing and desulfurization,Main component is carbon dioxide and steam, and the flue gas after purification is divided into three under the effect of flow control valvePoint: the circulating flue gas that Part I is oxygen-enriched combusting enters after flue gas oxygen mix device and oxygen mix as oneInferior wind, Secondary Air are sent into CFBC stove; Part II is that circulating flue gas passes into recirculating fluidized bed gasificationStove, for circle fluidized-bed gasification furnace provides the needed gas of gasification reaction and fluidized wind; Part III is for reclaimingFlue gas reclaims by flue gas recovery device; Two-way material controlling device fluidized wind, a material returning device fluidized wind, No. two returning chargesDevice fluidized wind all utilizes the high-temperature flue gas after purification.
Preferably, described CFBC stove running temperature is 900 DEG C～1200 DEG C, described ciculation fluidizedBed gasification furnace running temperature is 700 DEG C～900 DEG C.
Preferably, after described purification coal gas part as the fluidizing gas of described circle fluidized-bed gasification furnace.
Preferably, the fuel in described CFBC stove and the fuel in described circle fluidized-bed gasification furnaceFor coal, living beings or the main component solid fuel that is carbon.
Circulating fluid bed burning in oxygen enrichment polygenerations systeme provided by the invention compared with prior art, has following skillArt effect:
Existing recirculating fluidized bed polygenerations systeme combustion furnace adopts air burning, nitrogen in the tail flue gas of generationContent very large, if adopt flue gas as gasification furnace fluidizing gas, through gasification reaction produce synthesis gas masterWanting composition is nitrogen, and gas content is very low, if minority coal gas is separated from synthesis gas, efficiency is very low,Economical very poor, therefore can only adopt recirculation coal gas or steam as fluidizing gas, like this in gasification furnace onlyThe pyrolytic reaction that coal occurs there is not any reaction and is just admitted to combustion furnace in most coke in gas retortInterior burning, gas yield is very low, and part coal gas is used as fluidizing gas again, gas yield is lower, does not realizeThe efficient utilization of coal, and combustion furnace tail flue gas discharge capacity is very large.
In the present invention, CFBC stove adopts oxygen-enriched combusting, and in tail flue gas after treatment, main component isAccount for greatly 95% carbon dioxide and account for greatly 5% steam, such flue gas can be used as gasification furnaceFluidizing gas, the present invention has improved gasifier operation temperature, fuel in gasification furnace except normal pyrolytic reactionOutward, due to coke can also and fluidizing gas in carbon dioxide reaction generate carbon monoxide, carbon monoxide is coalOne of main component of gas, the coal gas amount that gasification furnace produces like this will significantly raise, and the utilization ratio of fuel raises,The partial fume that can not be utilized, because gas concentration lwevel is very high, is easy to reclaim, and cost recovery is very low.
The present invention is owing to having improved the reaction temperature in gasification furnace, and the gas temperature exporting at gasification furnace is far above JiaoOil Precipitation Temperature, at this moment passes through cyclone separator by coal gas, and Ceramic dust collector carries out slightly, thin two-stage ash disposal, thisThe burnt oil and gas dust burdening that sample reclaims is few, can reach commercial Application and civilian requirement.
Circulating fluid bed burning in oxygen enrichment polygenerations systeme provided by the invention and technique have overcome prior art notFoot, the utilization ratio of fuel is high, and gas yield is high, and quality of coke tar is good, and fuel and tail flue gas be profit to greatest extentWith, pollutant emission is few, and cost recovery is low.
Brief description of the drawings
Fig. 1 is circulating fluid bed burning in oxygen enrichment polygenerations systeme schematic diagram provided by the invention.
Detailed description of the invention
For the present invention is become apparent, hereby with a preferred embodiment, and coordinate accompanying drawing to be described in detail below.
Fig. 1 is circulating fluid bed burning in oxygen enrichment polygenerations systeme schematic diagram provided by the invention, described oxygen enrichment combustionBurn recirculating fluidized bed polygenerations systeme and comprise CFBC stove 1 and circle fluidized-bed gasification furnace 2, circulationFluid-bed combustion furnace 1 top is connected with a separator 3, and separator 3 top and back-end ductwork 13 connectConnect, No. one separator 3 bottoms are connected with two-way material controlling device 4, and two-way material controlling device 4 fires with recirculating fluidized bed respectivelyBurn stove 1 and be connected with circle fluidized-bed gasification furnace 2, circle fluidized-bed gasification furnace 2 by material returning device 5 with followRing fluid-bed combustion furnace 1 connects, and circle fluidized-bed gasification furnace 2 tops are connected with No. two separators 6, No. two pointsBe connected with circle fluidized-bed gasification furnace 2 by No. two material returning devices 7 from device 6 bottoms, No. two separator 6 tops andCeramic dust collector 18 connects, and Ceramic dust collector 18 connects gas cleaning system 8, and gas cleaning system 8 respectivelyBe connected with air accumulator 17 with tar pool 16. Back-end ductwork 13 by the out of stock device 11 of flue-gas dust-removing and desulfurization after withFlue gas distributing valve 14 is connected, and 14 outlets of flue gas distributing valve are divided into three tunnels, the first via and flue gas oxygen mix device10 are connected, and the second tunnel is connected with circle fluidized-bed gasification furnace 2, and Third Road is connected with flue gas recovery device 15,Air separator 9 is connected with nitrogen gas recovering apparatus 12 with flue gas oxygen mix device 10, flue gas oxygen mix dressPutting 10 bottoms is connected with CFBC stove 1.
The operation of circulating fluid bed burning in oxygen enrichment polygenerations systeme provided by the invention is as follows: air A warpAfter air separator 9 separates, obtain nitrogen B and oxygen C, nitrogen B reclaims by nitrogen gas recovering apparatus 12,Oxygen C with the circulating flue gas Q of oxygen-enriched combusting at interior even mixing of flue gas oxygen mix device 10, flue gas oxygenGaseous mixture D is divided into two-way and sends into CFBC stove 1 as wind E, a Secondary Air F respectively, onceWind E, Secondary Air F as oxidant and fluidized wind with together with fuel T in sending into CFBC stove 1Burning, the lime-ash V that burning generates discharges in CFBC stove 1 bottom, the flue gas G that burning generates(main component is carbon dioxide, steam, recycle stock) enters separator 3, most circulation No. oneMaterial is separated and enters two-way material controlling device 4 by a separator 3, under the regulating action of two-way material controlling device 4,A part is returned to CFBC stove 1, and another part enters circle fluidized-bed gasification furnace 2, enters gasificationThe high-temperature material J of stove provides circle fluidized-bed gasification furnace 2 fuel U gasification and the needed heat of pyrolytic reactionAmount. Control the high-temperature material amount and then the control that enter in circle fluidized-bed gasification furnace 2 by two-way material controlling device 4The temperature of circle fluidized-bed gasification furnace 2. The interior reacted semicoke mixtures of materials N of circle fluidized-bed gasification furnace 2Send into the interior after-flame of CFBC stove 1 through a material returning device 5. Circle fluidized-bed gasification furnace 2 tops go outThe untreated coal gas L coming enters separator 6 No. two, and the thin grey M being separated by No. two separators 6 passes throughNo. two material returning device 7 returns to circle fluidized-bed gasification furnace 2. The coal gas that go out on No. two separator 6 tops is first through potteryPorcelain deduster 18, then through gas cleaning system 8 interior dedusting, dewater, cooling, after separating carbon dioxide,Tar P is reclaimed by tar pool 16, and after purifying, coal gas O enters air accumulator 17, the tar P of recovery and purification coalGas O output is for industry and civilian, and if needed, the coal gas after purification also can partly be used as the stream of gasification furnace 2Oxidizing gases. Enter the flue gas of back-end ductwork 13 from separator 3 top through the out of stock dress of flue-gas dust-removing and desulfurizationAfter putting 11, main component is carbon dioxide and steam, and the flue gas H after purification is at flow control valve 14Under effect, be divided into three parts: the circulating flue gas Q that Part I is oxygen-enriched combusting enters flue gas oxygen mix device10 send into CFBC stove 1, Part II as wind E, a Secondary Air F after mixing with oxygen CFor circulating flue gas passes into circle fluidized-bed gasification furnace 2, for circle fluidized-bed gasification furnace 2 provides gasification reaction requiredThe gas of wanting and fluidized wind, Part III is that recovered flue gas S reclaims by flue gas recovery device 15. Two-way controlGlassware 4 fluidized wind W, material returning device 5 fluidized wind X, No. two material returning device 7 fluidized wind Y all utilize purificationAfter high-temperature flue gas. CFBC stove fuel T and gasification furnace fuel U are coal, living beings or masterWanting composition is the solid fuel of carbon.
Claims (5)
1. a circulating fluid bed burning in oxygen enrichment polygenerations systeme, is characterized in that: comprise CFBC stoveAnd circle fluidized-bed gasification furnace (2), CFBC stove (1) top and a separator (3) (1)Connect, a separator (3) top is connected with back-end ductwork (13), and a separator (3) bottom is with twoTo material controlling device (4) connect, two-way material controlling device (4) respectively with CFBC stove (1) and circular flowChange bed gasification furnace (2) and connect, circle fluidized-bed gasification furnace (2) is by a material returning device (5) and circular flowFluidized bed combustion stove (1) connects, and circle fluidized-bed gasification furnace (2) top is connected with No. two separators (6),No. two separators (6) bottom is connected with circle fluidized-bed gasification furnace (2) by No. two material returning devices (7), and twoNumber separator (6) top is connected with Ceramic dust collector (18), and Ceramic dust collector (18) connects gas purificationSystem (8), gas cleaning system (8) is connected with air accumulator (17) with tar pool (16) respectively; AfterbodyFlue (13) is connected with flue gas distributing valve (14) by after flue-gas dust-removing and desulfurization denitrification apparatus (11), flue gasDistributing valve (14) outlet is divided into three tunnels, and the first via is connected with flue gas oxygen mix device (10), the second tunnel andCircle fluidized-bed gasification furnace (2) is connected, and Third Road is connected with flue gas recovery device (15), air separator(9) be connected with nitrogen gas recovering apparatus (12) with flue gas oxygen mix device (10), flue gas oxygen mix dressPutting (10) bottom is connected with CFBC stove (1).
2. a circulating fluid bed burning in oxygen enrichment multi-production process, adopts oxygen-enriched combusting as claimed in claim 1 to followRing fluid bed polygenerations systeme, is characterized in that: air (A) obtains after air separator (9) separatesNitrogen (B) and oxygen (C), nitrogen (B) reclaims by nitrogen gas recovering apparatus (12), oxygen (C)In flue gas oxygen mix device (10), evenly mix flue gas oxygen with the circulating flue gas (Q) of oxygen-enriched combustingGaseous mixture (D) is divided into two-way and sends into CFBC as a wind (E), Secondary Air (F) respectivelyStove (1), a wind (E), Secondary Air (F) is as oxidant and fluidized wind and send into CFBCFuel (T) in stove (1) burns together, and the lime-ash (V) that burning generates is in CFBC stove (1)Discharge bottom, and the flue gas (G) that burning generates enters a separator (3), and most recycle stock is by oneNumber separator (3) separates and enters two-way material controlling device (4), under the regulating action of two-way material controlling device (4),A part is returned to CFBC stove (1), and another part enters circle fluidized-bed gasification furnace (2), entersThe high-temperature material (J) of gasification furnace provide circle fluidized-bed gasification furnace (2) fuel (U) gasification and pyrolysis anti-Answer needed heat; Control and enter in circle fluidized-bed gasification furnace (2) by two-way material controlling device (4)The temperature of high-temperature material amount and then controlled circulation fluidized-bed gasification furnace (2), in circle fluidized-bed gasification furnace (2)Reacted semicoke mixtures of materials (N) is sent into CFBC stove (1) through a material returning device (5)Interior after-flame, circle fluidized-bed gasification furnace (2) top untreated coal gas (L) out enters No. two separators (6),The thin ash (M) being separated by No. two separators (6) returns to recirculating fluidized bed by No. two material returning devices (7)Gasification furnace (2); The coal gas that go out on No. two separators (6) top first passes through Ceramic dust collector (18), then passes throughThe interior dedusting of gas cleaning system (8), dewater, cooling, after separating carbon dioxide, tar (P) is by tar pool(16) reclaim, after purifying, coal gas (O) enters air accumulator (17); Enter from a separator (3) topThe flue gas of back-end ductwork (13) is after flue-gas dust-removing and desulfurization denitrification apparatus (11), and main component is titanium dioxideCarbon and steam, the flue gas (H) after purification is divided into three parts under the effect of flue gas distributing valve (14): theThe circulating flue gas (Q) that a part is oxygen-enriched combusting enters flue gas oxygen mix device (10) and oxygen (C)After mixing, send into CFBC stove (1) as a wind (E), Secondary Air (F); Part II isCirculating flue gas passes into circle fluidized-bed gasification furnace (2), for circle fluidized-bed gasification furnace (2) provides gasification reactionNeeded gas and fluidized wind; Part III is that recovered flue gas (S) returns by flue gas recovery device (15)Receive; Two-way material controlling device fluidized wind (W), a material returning device fluidized wind (X), No. two material returning device fluidized winds (Y)All utilize the high-temperature flue gas after purifying.
3. a kind of circulating fluid bed burning in oxygen enrichment multi-production process as claimed in claim 2, is characterized in that: instituteStating CFBC stove running temperature is 900 DEG C～1200 DEG C, described circle fluidized-bed gasification furnace operation temperatureDegree is 700 DEG C～900 DEG C.
4. a kind of circulating fluid bed burning in oxygen enrichment multi-production process as claimed in claim 2, is characterized in that: instituteState and purify the fluidizing gas of rear coal gas (O) part as described circle fluidized-bed gasification furnace (2).
5. a kind of circulating fluid bed burning in oxygen enrichment multi-production process as claimed in claim 2, is characterized in that: instituteThe fuel (U) of stating in fuel (T) and the described circle fluidized-bed gasification furnace in CFBC stove isLiving beings or main component are the solid fuel of carbon.
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