CN203703950U - Oxygen-rich combustion circulating fluidized bed poly-generation system - Google Patents
Oxygen-rich combustion circulating fluidized bed poly-generation system Download PDFInfo
- Publication number
- CN203703950U CN203703950U CN201420041423.3U CN201420041423U CN203703950U CN 203703950 U CN203703950 U CN 203703950U CN 201420041423 U CN201420041423 U CN 201420041423U CN 203703950 U CN203703950 U CN 203703950U
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- CN
- China
- Prior art keywords
- fluidized bed
- flue gas
- circulating fluidized
- gasification furnace
- separator
- 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.)
- Withdrawn - After Issue
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 239000001301 oxygen Substances 0.000 title claims abstract description 32
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 32
- 238000002485 combustion reaction Methods 0.000 title abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000003546 flue gas Substances 0.000 claims abstract description 45
- 238000002309 gasification Methods 0.000 claims abstract description 43
- 239000000463 material Substances 0.000 claims abstract description 26
- 239000000428 dust Substances 0.000 claims abstract description 13
- 239000000919 ceramic Substances 0.000 claims abstract description 9
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 31
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 11
- 238000004140 cleaning Methods 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 4
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- 239000003034 coal gas Substances 0.000 abstract description 16
- 239000000446 fuel Substances 0.000 abstract description 13
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000002641 tar oil Substances 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000000203 mixture Substances 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 239000011269 tar Substances 0.000 description 9
- 230000001276 controlling effect Effects 0.000 description 8
- 239000001569 carbon dioxide Substances 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 239000000571 coke Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 239000000126 substance 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
- 230000000694 effects Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 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
- 238000002156 mixing Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000004449 solid propellant Substances 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 utility model provides an oxygen-rich combustion circulating fluidized bed poly-generation system. The oxygen-rich combustion circulating fluidized bed poly-generation system comprises a circulating fluidized bed combustion furnace and a circulating fluidized bed gasification furnace, wherein the circulating fluidized bed combustion furnace is connected with a first separator; the first separator is connected with a tail chimney flue and a two-way material control device; the two-way material control device is connected with the circulating fluidized bed combustion furnace and the circulating fluidized bed gasification furnace respectively; the circulating fluidized bed gasification furnace is connected with the circulating fluidized bed combustion furnace through a first refeeding device, and is connected with a ceramic dust collector and a coal gas purifying system through a second separator; the tail chimney flue is connected with a flue gas distributing valve after passing a flue gas dust removing desulfuration and denitration device; the outlet of the flue gas distributing valve is divided into three ways. The system is high in utilization efficiency of fuel, high in coal gas production, and good in tar oil quality; the fuel and the tail flue gas are utilized to the utmost extent; the pollutant emission as well as the recycling cost is low.
Description
Technical field
The utility model relates to a kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme, belongs to coal Poly-generation technology field.
Background technology
China is lower to the utilization ratio of existing resource at present, and especially, aspect coal fired power generation or power station heat supply, energy conversion efficiency is lower than 40%, and aspect the chemical industry such as coking, oil refining, the utilization ratio of coal is relatively high, can reach 85%～90%.Clean and effective utilizes coal resources, advances coal Poly-generation to become one of primary study direction of national strategy.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 chemical by-product of gaseous fuel and multiple high added value, realizes that coal utilization is the most efficient, minimum pollution.Evidence, power industry adopts polygenerations systeme, and generating efficiency can improve approximately 10%, and cost declines 30%, and polygenerations systeme also makes the production cost of chemical products significantly reduce simultaneously.
Chinese utility model patent 200610154581.X provides a kind of circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method thereof, be made up of fluid-bed combustion furnace, fluidized bed dry distillation stove, high-temperature separator, material returning device and corresponding auxiliary device, product is mainly coal gas and tar.Fluidized bed dry distillation stove adopts recirculation coal gas or steam as fluidizing gas, in gas retort, temperature is on the low side, only there is the pyrolytic reaction of coal, in gas retort, there is not any reaction and be just admitted in combustion furnace and burn in most coke, gas yield is very low, and part coal gas is used as fluidizing gas again, gas yield is lower; The tar yield that fluidized bed dry distillation stove produces is higher, but tar is difficult to separate with dust, and tar product dust burdening is difficult to greatly realize commercial Application.
Utility model content
It is high that the technical problems to be solved in the utility model is to provide a kind of gas yield, and tail flue gas can recycling, and the circulating fluid bed burning in oxygen enrichment polygenerations systeme that pollutant emission is low is really realized the most efficient, minimum pollution of fuel utilization.
In order to solve the problems of the technologies described above, the technical solution of the utility model is to provide a kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme, it is characterized in that: comprise CFBC stove and circle fluidized-bed gasification furnace, CFBC stove top is connected with a separator, No. one separator top is connected with back-end ductwork, No. one separator bottom is connected with two-way material controlling device, 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 top is connected with No. two separators, No. two separator bottom is connected with circle fluidized-bed gasification furnace by No. two material returning devices, No. two separator top is connected with Ceramic dust collector, Ceramic dust collector connects gas cleaning system, gas cleaning system is connected with air accumulator with tar pool respectively, 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 first via is connected with flue gas oxygen mix device, the second tunnel is connected with circle fluidized-bed gasification furnace, Third Road is connected with flue gas recovery device, air separator is connected with nitrogen gas recovering apparatus with flue gas oxygen mix device, and flue gas oxygen mix device bottom is connected with CFBC stove.
The circulating fluid bed burning in oxygen enrichment polygenerations systeme that the utility model provides compared with prior art, has following technique effect:
Existing recirculating fluidized bed polygenerations systeme combustion furnace adopts air burning, in the tail flue gas producing, the content of nitrogen is very large, if adopt flue gas as gasification furnace fluidizing gas, the synthesis gas main component producing through gasification reaction is nitrogen, 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, in gasification furnace, only there is like this pyrolytic reaction of coal, in gas retort, there is not any reaction and be just admitted in combustion furnace and burn in most coke, gas yield is very low, and part coal gas is again as fluidizing gas, gas yield is lower, do not realize the efficient utilization of coal, and combustion furnace tail flue gas discharge capacity is very large.
In the utility model, CFBC stove adopts oxygen-enriched combusting, in tail flue gas after treatment, main component is account for greatly 95% carbon dioxide and account for greatly 5% steam, such flue gas can be used as the fluidizing gas of gasification furnace, the utility model has improved gasifier operation temperature, fuel in gasification furnace except normal pyrolytic reaction, due to coke can also and fluidizing gas in carbon dioxide reaction generate carbon monoxide, carbon monoxide is one of main component of coal gas, the coal gas amount that gasification furnace produces like this will significantly raise, the utilization ratio of fuel raises, the partial fume that can not be utilized is because gas concentration lwevel is very high, be easy to reclaim, cost recovery is very low.
The utility model is owing to having improved the reaction temperature in gasification furnace, the gas temperature exporting at gasification furnace is far above tar Precipitation Temperature, at this moment coal gas is passed through to cyclone separator, Ceramic dust collector carries out slightly, thin two-stage ash disposal, the burnt oil and gas dust burdening reclaiming is like this few, can reach commercial Application and civilian requirement.
The circulating fluid bed burning in oxygen enrichment polygenerations systeme that the utility model provides has overcome the deficiencies in the prior art, and 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 utilize to greatest extent, and pollutant emission is few, and cost recovery is low.
Accompanying drawing explanation
The circulating fluid bed burning in oxygen enrichment polygenerations systeme schematic diagram that Fig. 1 provides for the utility model.
The specific embodiment
For the utility model is become apparent, hereby with a preferred embodiment, and coordinate accompanying drawing to be described in detail below.
The circulating fluid bed burning in oxygen enrichment polygenerations systeme schematic diagram that Fig. 1 provides for the utility model, described circulating fluid bed burning in oxygen enrichment polygenerations systeme comprises CFBC stove 1 and circle fluidized-bed gasification furnace 2, CFBC stove 1 top is connected with a separator 3, No. one separator 3 tops are connected with back-end ductwork 13, No. one separator 3 bottoms are connected with two-way material controlling device 4, two-way material controlling device 4 is connected with CFBC stove 1 and circle fluidized-bed gasification furnace 2 respectively, circle fluidized-bed gasification furnace 2 is connected with CFBC stove 1 by a material returning device 5, circle fluidized-bed gasification furnace 2 tops are connected with No. two separators 6, No. two separator 6 bottoms are connected with circle fluidized-bed gasification furnace 2 by No. two material returning devices 7, No. two separator 6 tops are connected with Ceramic dust collector 18, Ceramic dust collector 18 connects gas cleaning system 8, gas cleaning system 8 is connected with air accumulator 17 with tar pool 16 respectively.Back-end ductwork 13 is connected with flue gas distributing valve 14 by after the out of stock device 11 of flue-gas dust-removing and desulfurization, 14 outlets of flue gas distributing valve are divided into three tunnels, the first via is connected with flue gas oxygen mix device 10, the second tunnel is connected with circle fluidized-bed gasification furnace 2, 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, and flue gas oxygen mix device 10 bottoms are connected with CFBC stove 1.
The operation of the circulating fluid bed burning in oxygen enrichment polygenerations systeme that the utility model provides is as follows: air A obtains nitrogen B and oxygen C after air separator 9 separates, nitrogen B reclaims by nitrogen gas recovering apparatus 12, oxygen C with the circulating flue gas Q of oxygen-enriched combusting in interior even mixing of flue gas oxygen mix device 10, flue gas oxygen mixture D is divided into two-way respectively as a wind E, Secondary Air F sends into CFBC stove 1, a wind E, Secondary Air F burns with together with fuel T in sending into CFBC stove 1 as oxidant and fluidized wind, the lime-ash V that burning generates discharges in CFBC stove 1 bottom, (main component is carbon dioxide to the flue gas G that burning generates, steam, recycle stock) enter separator 3 No. one, most recycle stock 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, another part enters circle fluidized-bed gasification furnace 2, the high-temperature material J that enters gasification furnace provides circle fluidized-bed gasification furnace 2 fuel U gasification and the needed heats of pyrolytic reaction.Control the high-temperature material amount that enters in circle fluidized-bed gasification furnace 2 and then the temperature of controlled circulation fluidized-bed gasification furnace 2 by two-way material controlling device 4.The interior reacted semicoke mixtures of materials N of circle fluidized-bed gasification furnace 2 sends into the interior after-flame of CFBC stove 1 through a material returning device 5.Circle fluidized-bed gasification furnace 2 tops untreated coal gas L out enters separator 6 No. two, and the thin grey M being separated by No. two separators 6 returns to circle fluidized-bed gasification furnace 2 by No. two material returning devices 7.The coal gas that go out on No. two separator 6 tops first passes through Ceramic dust collector 18, again through gas cleaning system 8 interior dedusting, dewater, cooling, after separating carbon dioxide, tar P is reclaimed by tar pool 16, after purifying, coal gas O enters air accumulator 17, the tar P reclaiming is with purification coal gas O output for industry and civilian, and if needed, the coal gas after purification also can partly be used as the fluidizing gas of gasification furnace 2.The flue gas that enters back-end ductwork 13 from separator 3 top is after the out of stock device 11 of flue-gas dust-removing and desulfurization, main component is carbon dioxide and steam, flue gas H after purification is divided into three parts under the effect of flow control valve 14: the circulating flue gas Q that Part I is oxygen-enriched combusting enters flue gas oxygen mix device 10 mix with oxygen C after as a wind E, Secondary Air F sends into CFBC stove 1, Part II is that circulating flue gas passes into circle fluidized-bed gasification furnace 2, for circle fluidized-bed gasification furnace 2 provides the needed gas of gasification reaction and fluidized wind, Part III is that recovered flue gas S reclaims by flue gas recovery device 15.Two-way material controlling device 4 fluidized wind W, material returning device 5 fluidized wind X, No. two material returning device 7 fluidized wind Y all utilize the high-temperature flue gas after purification.CFBC stove fuel T and gasification furnace fuel U are that coal, living beings or main component are the solid fuel of carbon.
Claims (1)
1. a circulating fluid bed burning in oxygen enrichment polygenerations systeme, it is characterized in that: comprise CFBC stove (1) and circle fluidized-bed gasification furnace (2), CFBC stove (1) top is connected with a separator (3), a separator (3) top is connected with back-end ductwork (13), a separator (3) bottom is connected with two-way material controlling device (4), two-way material controlling device (4) is connected with CFBC stove (1) and circle fluidized-bed gasification furnace (2) respectively, circle fluidized-bed gasification furnace (2) is connected with CFBC stove (1) by a material returning device (5), 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), No. two separators (6) top is connected with Ceramic dust collector (18), Ceramic dust collector (18) connects gas cleaning system (8), gas cleaning system (8) is connected with air accumulator (17) with tar pool (16) respectively, back-end ductwork (13) is connected with flue gas distributing valve (14) by after the out of stock device of flue-gas dust-removing and desulfurization (11), flue gas distributing valve (14) outlet is divided into three tunnels, the first via is connected with flue gas oxygen mix device (10), the second tunnel is connected with circle fluidized-bed gasification furnace (2), 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), and flue gas oxygen mix device (10) bottom is connected with CFBC stove (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420041423.3U CN203703950U (en) | 2014-01-23 | 2014-01-23 | Oxygen-rich combustion circulating fluidized bed poly-generation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420041423.3U CN203703950U (en) | 2014-01-23 | 2014-01-23 | Oxygen-rich combustion circulating fluidized bed poly-generation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203703950U true CN203703950U (en) | 2014-07-09 |
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|---|---|---|---|
| CN201420041423.3U Withdrawn - After Issue CN203703950U (en) | 2014-01-23 | 2014-01-23 | Oxygen-rich combustion circulating fluidized bed poly-generation system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103742899A (en) * | 2014-01-23 | 2014-04-23 | 上海锅炉厂有限公司 | Oxygen-enriched combustion circulating fluidized bed poly-generation system and process |
-
2014
- 2014-01-23 CN CN201420041423.3U patent/CN203703950U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103742899A (en) * | 2014-01-23 | 2014-04-23 | 上海锅炉厂有限公司 | Oxygen-enriched combustion circulating fluidized bed poly-generation system and process |
| CN103742899B (en) * | 2014-01-23 | 2016-05-04 | 上海锅炉厂有限公司 | A kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140709 Effective date of abandoning: 20160504 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |