CN204939411U - The hot analytical system of a kind of fluidized bed coal - Google Patents
The hot analytical system of a kind of fluidized bed coal Download PDFInfo
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- CN204939411U CN204939411U CN201520499924.0U CN201520499924U CN204939411U CN 204939411 U CN204939411 U CN 204939411U CN 201520499924 U CN201520499924 U CN 201520499924U CN 204939411 U CN204939411 U CN 204939411U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The utility model discloses the hot analytical system of a kind of fluidized bed coal, comprising: multicompartment fluidized bed reactor, be provided with coal inlet, preheated air and water vapor mixing entrance, mixed gas outlet, semicoke returning charge mouth and semicoke outlet; The mixed gas outlet of multicompartment fluidized bed reactor is connected with gas-solid separator, waste heat boiler and water wash column successively; Waste heat boiler is provided with steam outlet, and this steam entry is connected with mixing tank and air preheater respectively; Air preheater is connected with mixing tank, and the outlet of mixing tank is connected with the preheated air of multicompartment fluidized bed reactor and water vapor mixing entrance.By adopting multicompartment fluidized bed reactor, bed temperature is stablized, and there is not thermograde, solves axial in stove and that radial temperature profile is uneven technological deficiency; Achieve pyrolysis and gasification PROCESS COUPLING in multicompartment fluidized bed reactor, high-temperature gasification coal gas adverse current and coal directly carry out gas-particle two-phase and contact, and carry out pyrolysis of coal conversion, and caloric power of gas improves, and in technique, heat transfer efficiency is high, and total energy utilization ratio is high.
Description
Technical field
The utility model relates to pyrolysis of coal field, particularly relates to the hot analytical system of a kind of fluidized bed coal.
Background technology
" oil-poor, weak breath, relative rich coal " is the current Energy Situation of China.Along with the high speed development of Chinese national economy and improving constantly of living standards of the people, the imbalance between supply and demand of primary energy source PetroChina Company Limited. becomes increasingly conspicuous, Chinese crude oil net importation amount 3.1 hundred million tons in 2014,59.6% is reached to the interdependency of overseas oil, and by the restriction in national power and foreign exchange, China is difficult to support so large-scale petroleum import, and national energy security cannot ensure, oil and gas gap problem urgently to be resolved hurrily.Compared with oil, the proportion that coal in China output and consumption account in primary energy source remains on about 70% always, how Development of Novel Coal Chemical Industry, builds large-scale New Coal Chemical Poly-generation project, produces the vital task that oil replacement product is becoming China's energy construction.
Coal fast pyrolysis process can obtain high-quality tar under comparatively mild conditions, and clean semicoke and coal gas, high-quality tar can hydrofining be the Chemicals such as light-end products.Mostly pyrolysis of coal process is thermo-negative reaction, traditional technology to be the mode solving pyrolysis of coal process need heat be solid thermal carriers heat supply (the Lurgi-ruhr-gas technique etc. as the DG pyrolytic process of Dalian University of Technology, Oil Shale Corporation of America TOSCOAL technique, German Rule LURGI) or gaseous heat-carrier heat supply (as vertical heater technique, multistage rotary kiln technique etc.).The reaction heat heat solid thermal barrier that solid thermal carriers heat supply generally adopts combustion parts pyrolysis char to discharge is pyrolytic process heat supply by gas-solid separating device heat of dissociation carrier; The heat smoke that gaseous heat-carrier heat supply then generally adopts combustion parts semicoke or pyrolysis coal gas to produce is pyrolytic process heat supply.Figure 1 shows that the technical scheme of existing solid thermal carriers technique; broken coal enters pyrolysis unit (fluidized-bed, down-flow fluidized bed using ECT or moving-bed) by feeding unit; the thermal barrier particle heated with burned unit (circulating fluidized bed) mixes; raw pyrolytic reaction is issued the temperature of 500 ~ 650 DEG C; generate pyrolysis coal gas, tar and semicoke; wherein the returning charge of part semicoke is to fuel element; at the temperature of 900 ~ 950 DEG C, combustion reactions occurs, the reaction heat of generation is used for heat solid thermal barrier for pyrolytic reaction provides heat.At present, the Lurgi-ruhr-gas technique etc. of the DG pyrolytic process of Dalian University of Technology, Oil Shale Corporation of America TOSCOAL technique, German Rule LURGI is all typically used of solid thermal carriers technique.The shortcoming of the program is: solid thermal carriers heat supply generally adopts double bed pyrolytic process, invests high, and thermal barrier adopts circulating fluidized bed to heat at fuel element, apparatus body high (tens meters of rice even up to a hundred), and equipment operation energy consumption is high; Meanwhile, technique pyrolysis char when carrying out pyrolysis mixes mutually with thermal barrier, and semicoke separating-purifying exists difficulty.
Solid thermal carriers heat supply generally adopts double bed pyrolytic process, invests high, and thermal barrier adopts circulating fluidized bed to heat, apparatus body higher (tens meters of rice even up to a hundred), and equipment operation energy consumption is high; Meanwhile, technique pyrolysis char when carrying out pyrolysis mixes mutually with thermal barrier, and semicoke separating-purifying exists difficulty; Gaseous heat-carrier heat supply generally adopts vertical heater technique and multistage rotary kiln technique at present, and facility investment is few.But vertical heater technique belongs to moving-bed, to exist in stove axially and radial temperature profile uneven, be easy to coking; Meanwhile, too simple owing to producing, auxiliary facility is few, and environmental pollution is serious, and each place government has started to rectify; Multistage rotary kiln technique adopts the space combustion partial thermal decomposition coal gas between distil container outer wall and Inner Wall of Combustion Chamber to produce high-temperature hot flue gas, and with heat exchange pattern to pyrolytic process indirect heating, heat transfer efficiency is low, technique total energy utilization ratio is low.Figure 2 shows that existing gaseous heat-carrier process technology scheme, in vertical heater technique, coal occur successively from top to bottom in vertical heater drying, pyrolysis, combustion reactions, produce coal gas and tar is discharged by furnace roof, semicoke is arranged outward by furnace bottom.The heat smoke that pyrolytic process institute heat requirement is produced by burning zone combustion parts semicoke directly contacts heat supply with coal, as shown in Fig. 2 (I).In multistage rotary kiln technique, coal carries out pyrolysis in multi-stage series rotary kiln, finally obtains the tar of higher yields, pyrolysis coal gas and semicoke.Wherein, the high-temperature hot flue gas that coal is produced by combustion parts pyrolysis coal gas in pyrolytic process institute heat requirement, by heat exchange pattern for pyrolysis of coal in rotary kiln provides heat, as shown in Fig. 2 (II).The shortcoming of the program is: vertical heater technique belongs to moving-bed, and stove is axially interior and radial temperature profile is uneven, is easy to coking; Meanwhile, too simple owing to producing, auxiliary facility is few, and environmental pollution is serious; Multistage rotary kiln technique adopts the space combustion partial thermal decomposition coal gas between distil container outer wall and Inner Wall of Combustion Chamber to produce high-temperature hot flue gas, and with heat exchange pattern to pyrolytic process indirect heating, heat transfer efficiency is low, technique total energy utilization ratio is low.
Utility model content
Based on the problem existing for above-mentioned prior art, the utility model provides a kind of fluidized bed coal hot analytical system, directly can realize three coproduction of high-quality pyrolysis gas, semicoke and tar, overcomes the low shortcoming of existing pyrolytic process semicoke purification & isolation, coking and thermo-efficiency in fluidized-bed.
For solving the problems of the technologies described above, the utility model provides a kind of fluidized bed coal hot analytical system, comprising:
Multicompartment fluidized bed reactor, gas-solid separator, mixing tank, air preheater, waste heat boiler and water wash column, wherein,
Described multicompartment fluidized bed reactor, is provided with coal inlet, preheated air and water vapor mixing entrance, mixed gas outlet, semicoke returning charge mouth and semicoke outlet;
The mixed gas outlet of described multicompartment fluidized bed reactor is connected with described gas-solid separator, waste heat boiler and water wash column successively;
Described gas-solid separator is provided with mixed gas relief outlet and semicoke outlet, and this mixed gas relief outlet is connected with described waste heat boiler, and the outlet of this semicoke is connected with the semicoke returning charge mouth of described multicompartment fluidized bed reactor;
Described waste heat boiler is provided with steam outlet, and this steam outlet is connected with described mixing tank and described air preheater respectively;
Described air preheater is connected with described mixing tank, and the outlet of described mixing tank is connected with the preheated air of described multicompartment fluidized bed reactor and water vapor mixing entrance.
The beneficial effects of the utility model are: by adopting multicompartment fluidized bed reactor, fluidized-bed bed temperature-stable, does not exist thermograde substantially, solve gaseous heat-carrier pyrolytic process and there is axial in stove and that radial temperature profile is uneven technological deficiency; And achieving pyrolysis and gasification PROCESS COUPLING in multicompartment fluidized bed reactor, high-temperature gasification coal gas adverse current and coal directly carry out gas-particle two-phase and contact, and carry out pyrolysis of coal conversion, and caloric power of gas improves, and in technique, heat transfer efficiency is high, and total energy utilization ratio is high.This system investments is low, equipment operation energy consumption is low, there is not semicoke and thermal barrier separating-purifying problem, solves technological deficiency that solid thermal carriers technique exists (as semicoke and thermal barrier separating-purifying difficulty is large, cost of investment is high, equipment operation energy consumption is high).
Accompanying drawing explanation
In order to be illustrated more clearly in the technical scheme of the utility model embodiment, below the accompanying drawing used required in describing embodiment is briefly described, apparently, accompanying drawing in the following describes is only embodiments more of the present utility model, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the schematic diagram of existing solid thermal carriers technique;
The schematic diagram of Fig. 2 (I), (II) all existing gaseous heat-carrier technique;
The structural representation of the system of the multicompartment fluidized bed pyrolysis of coal that Fig. 3 provides for the utility model embodiment.
Embodiment
Be clearly and completely described the technical scheme in the utility model embodiment below, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiments.Based on embodiment of the present utility model, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to protection domain of the present utility model.
As shown in Figure 3, the system of a kind of multicompartment fluidized bed pyrolysis of coal of the utility model embodiment, comprising: multicompartment fluidized bed reactor 1, mixing tank 5, air preheater 6, gas-solid separator 2, waste heat boiler 3 and water wash column 4,
Wherein, multicompartment fluidized bed reactor 1, is provided with coal inlet 11, preheated air and water vapor mixing entrance 14, mixed gas outlet 12, semicoke returning charge mouth 15 and semicoke outlet 13;
The mixed gas outlet 12 of multicompartment fluidized bed reactor 1 is connected with gas-solid separator 2, waste heat boiler 3 and water wash column 4 successively;
Gas-solid separator 2 is provided with mixed gas relief outlet and semicoke outlet, and this mixed gas relief outlet is connected with waste heat boiler 3, and the outlet of this semicoke is connected with the semicoke returning charge mouth 15 of multicompartment fluidized bed reactor;
Waste heat boiler 3 is provided with steam outlet, and this steam outlet is connected with mixing tank 5 and air preheater 6 respectively;
Air preheater 6 is connected with mixing tank 5, and the outlet of mixing tank 5 is connected with the preheated air of multicompartment fluidized bed reactor 1 and water vapor mixing entrance 14.
In said system, at the external gas-solid separating device of multicompartment fluidized bed reactor, fine breeze under being separated enters bottom multicompartment fluidized bed and participates in gasification reaction, solving because containing a large amount of fine breezes in mixed gas, to the dedusting of follow-up waste heat boiler and the problem that impact can be run in multicompartment fluidized bed is produced.
In said system, multicompartment fluidized bed reactor sets gradually at least three laminarization bed beds in it from top to bottom, and preferably arrange seven laminarization bed beds, those skilled in the art can know, the number of plies of multicompartment fluidized bed reactor is not limited only to seven layers, also can adopt the multicompartment fluidized bed of other numbers of plies.
The returning charge valve that in the multicompartment fluidized bed reactor of said system, every laminarization bed is arranged all is arranged around the periphery of this laminarization bed.
In said system, the coal inlet of multicompartment fluidized bed reactor and mixed gas export the top being located at multicompartment fluidized bed reactor body respectively, semicoke outlet and semicoke returning charge mouth are located at the bottom of multicompartment fluidized bed reactor body, and preheated air and water vapor mixing entrance are located at the bottom of multicompartment fluidized bed reactor body.
Further, said system also comprises: apparatus for feeding, is connected with the coal inlet of multicompartment fluidized bed reactor.
Below in conjunction with pyrolysis of coal process, system of the present utility model is described further.
As shown in Figure 3, in the pyrolysis of coal method utilizing this system to carry out, coal A enters multicompartment fluidized bed reactor 1 top by apparatus for feeding (as feeding screw etc.), the pyrolytic process of coal is completed in each laminarization bed, the gasification gas that pyrolytic process institute heat requirement carries out air+steam gasification generation primarily of pyrolysis char in multicompartment fluidized bed reactor orlop reactor provides, gasification temperature controls at 850 ~ 950 DEG C, produce coal gas composition: CO (19.6 ~ 22%), CO2 (9.9 ~ 13.4%), H2 (11.9 ~ 17.5%), CH4 (0.7 ~ 3.4%), N2 (48.9 ~ 55.3%).In char Gasification process, produce high-temperature gasification coal gas and in each fluidized-bed, directly carry out gas-particle two-phase by fluidized bed air distribution plate and coal successively from bottom to top and contact, carry out the converting of coal, pyrolysis temperature controls at 600 ~ 800 DEG C, after pyrolysis, gasification gas mixes with pyrolysis coal gas, and mixed gas consists of: CO (10.1 ~ 12.2%), CO2 (2.5 ~ 4.7%), H2 (44.0 ~ 51.4%), CH4 (1.6 ~ 2.8%), N2 (30.5 ~ 39.5%).Simultaneously, tar that pyrolytic process generates then enters waste heat boiler and water B heat exchange produces high temperature super heated steam with pyrolytic gasification mixed gas in multicompartment fluidized bed reactor head after gas-solid separator gas solid separation, wherein a part is as the vaporized chemical of multicompartment fluidized bed reactor orlop reactor, all the other then enter air preheater preheated air E, water F discharged by air preheater, preheated air and enter the air compartment of multicompartment fluidized bed as the superheated vapour of vaporized chemical through mixing tank.Directly cool through water wash column further through the tar of residual heat boiler for exchanging heat and pyrolytic gasification mixed gas, realize being separated of tar D and mixed gas C; Every laminarization bed carry out converting after semicoke then through the returning charge from top to bottom of returning charge valve to participating in char Gasification reaction in undermost fluidized-bed reactor, under the condition maintaining the required bed height of orlop fluidized-bed reactor reaction, control returning charge valve returning charge air quantity semicoke product G is discharged through revert pipe, thus realize mixed gas C, tar D and semicoke G tri-coproduction of pyrolysis of coal process, as shown in Figure 3.
System of the present utility model adopts multicompartment fluidized bed, and fully, bed temperature is stablized, and substantially there is not thermograde in gas-particle two-phase contact; Achieve three coproduction of calorific value of gas in pyrolysis of coal process, high-quality semicoke and tar, and achieve pyrolysis and gasification PROCESS COUPLING in stove, heat transfer efficiency is high, and total energy utilization ratio is high, and technology investment is low, equipment operation energy consumption is low, there is not semicoke and thermal barrier separating-purifying problem; There is semicoke and thermal barrier separating-purifying difficulty is large, cost of investment is high, equipment operation energy consumption is high technical problem in the pyrolysis of coal system solving solid thermal carriers technique, solve simultaneously existing gaseous heat-carrier pyrolytic process to exist in stove axially and radial temperature profile inequality, heat transfer efficiency low, the technical problem that technique total energy utilization ratio is low.
The above; be only the utility model preferably embodiment; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; the change that can expect easily or replacement, all should be encompassed within protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims.
Claims (6)
1. the hot analytical system of fluidized bed coal, is characterized in that, comprising:
Multicompartment fluidized bed reactor, gas-solid separator, mixing tank, air preheater, waste heat boiler and water wash column, wherein,
Described multicompartment fluidized bed reactor, is provided with coal inlet, preheated air and water vapor mixing entrance, mixed gas outlet, semicoke returning charge mouth and semicoke outlet;
The mixed gas outlet of described multicompartment fluidized bed reactor is connected with described gas-solid separator, waste heat boiler and water wash column successively;
Described gas-solid separator is provided with mixed gas relief outlet and semicoke outlet, and this mixed gas relief outlet is connected with described waste heat boiler, and the outlet of this semicoke is connected with the semicoke returning charge mouth of described multicompartment fluidized bed reactor;
Described waste heat boiler is provided with steam outlet, and this steam outlet is connected with described mixing tank and described air preheater respectively;
Described air preheater is connected with described mixing tank, and the outlet of described mixing tank is connected with the preheated air of described multicompartment fluidized bed reactor and water vapor mixing entrance.
2. the hot analytical system of a kind of fluidized bed coal according to claim 1, is characterized in that, sets gradually at least three laminarization bed beds in described multicompartment fluidized bed reactor from top to bottom.
3. the hot analytical system of a kind of fluidized bed coal according to claim 1 and 2, is characterized in that, sets gradually seven laminarization bed beds in described multicompartment fluidized bed reactor from top to bottom.
4. the hot analytical system of a kind of fluidized bed coal according to claim 1 and 2, is characterized in that, the returning charge valve that in described multicompartment fluidized bed reactor, every laminarization bed is arranged all is arranged around the periphery of this laminarization bed.
5. the hot analytical system of a kind of fluidized bed coal according to claim 1 and 2, it is characterized in that, coal inlet and the gas using residual heat of described multicompartment fluidized bed reactor export the top being located at described multicompartment fluidized bed reactor body respectively, described semicoke outlet and semicoke returning charge mouth are located at the bottom of described multicompartment fluidized bed reactor body, and described preheated air and water vapor mixing entrance are located at the bottom of described multicompartment fluidized bed reactor body.
6. the hot analytical system of a kind of fluidized bed coal according to claim 1 and 2, is characterized in that, also comprise: apparatus for feeding, is connected with the coal inlet of described multicompartment fluidized bed reactor.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107892950A (en) * | 2017-11-08 | 2018-04-10 | 中科合肥煤气化技术有限公司 | A kind of high temperature heating gas waste-heat recovery device |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
| CN114717017A (en) * | 2022-05-09 | 2022-07-08 | 孙孝德 | Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal |
-
2015
- 2015-07-10 CN CN201520499924.0U patent/CN204939411U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107892950A (en) * | 2017-11-08 | 2018-04-10 | 中科合肥煤气化技术有限公司 | A kind of high temperature heating gas waste-heat recovery device |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
| CN114717017A (en) * | 2022-05-09 | 2022-07-08 | 孙孝德 | Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal |
| CN114717017B (en) * | 2022-05-09 | 2022-12-06 | 孙孝德 | Two-stage fluidized pyrolysis integrated furnace and method for preparing semi-coke from low-rank crushed coal |
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Effective date of registration: 20210726 Address after: 426191 room 409, office building of Commerce and Grain Bureau, Jindong Management District, Yongzhou City, Hunan Province Patentee after: Yongzhou Qidi leihao new energy Co.,Ltd. Address before: 100083 a-405, Tiangong building, Keda, 30 Xueyuan Road, Haidian District, Beijing Patentee before: BEIJING LEIHAO ENVIRONMENTAL PROTECTION ENERGY TECHNOLOGY Co.,Ltd. |
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