CN105670664A - Pulverized coal pyrolysis device - Google Patents
Pulverized coal pyrolysis device Download PDFInfo
- Publication number
- CN105670664A CN105670664A CN201610193143.8A CN201610193143A CN105670664A CN 105670664 A CN105670664 A CN 105670664A CN 201610193143 A CN201610193143 A CN 201610193143A CN 105670664 A CN105670664 A CN 105670664A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- venting port
- pulverized coal
- outlet
- settling pocket
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention provides a pulverized coal pyrolysis device which comprises a rotary radiation bed, a hot-blast stove and a smoke ejector, wherein the rotary radiation bed is provided with a pulverized coal feed port, a thermal medium inlet, a thermal medium outlet, a semi-coke outlet and a crude gas exhaust port; the hot-blast stove is provided with a semi-coke inlet and a hot air exhaust port; the semi-coke inlet is communicated with the semi-coke outlet in the rotary radiation bed; the smoke ejector is provided with a hot air inlet, an ejection gas inlet and an ejector exit; the hot air inlet is communicated with the hot air exhaust port in the hot-blast stove; the ejector exit is communicated with the thermal medium inlet; and the ejection gas inlet is communicated with the thermal medium outlet in the rotary radiation bed. In the device, the semi-coke is burnt in the hot-blast stove, and the generated high-temperature smoke returns to the rotary radiation bed to supply pyrolysis heat; and thus, the utilization of the semi-coke heat is facilitated to solve the problem of difficulty in semi-coke treatment. Meanwhile, the high-temperature smoke is ejected into the rotary radiation bed by the smoke ejector, the gas pressure can be increased, and the problem of dust blocking of thermal medium channel or low heat exchange efficiency is avoided.
Description
Technical field
The present invention relates to pulverized coal pyrolysis technical field, specifically, it relates to a kind of pulverized coal pyrolysis device.
Background technology
Fine coal (also known as foam coal, or low-rank coal) it is the necessary byproduct produced in progress of coal mining, the use of especially modern performing comprehensive coal mining equipment more increases the output of foam coal. And China is relatively strong to the dependency of coal resources, fine coal development of resources and clean utilization being paid attention to gradually at present, this maintains China's sustainable economic development, ensures the important behave of energy security developments.
In current published technology, such as coal liquifaction, coal preparing natural gas; the technology such as ammonia from coal; or adopting the technology of low temperature, middle gentle high temperature coke, gas, the particle of the raw coal of employing is substantially at more than 25mm, and fine coal particle diameter being less than to 25mm is then more difficult. Meanwhile, existing pyrolytic technique processing power is little, cannot meet big suitability for industrialized production, and economic benefit and the feature of environmental protection are poor, and social benefit is not remarkable. Above-mentioned various reasons causes fine coal bulk deposition, cannot produce economic benefit, causes new environmental issue simultaneously. Therefore, the clean utilization of fine coal has become the difficult problem that is needed badly solution.
Prior art is for, in the treatment process of fine coal, pulverized coal pyrolysis technique can realize the clean and effective to fine coal and utilize, and its pyrolysis product has tar, pyrolysis coal gas, high heating value semicoke etc. Currently there will be a known multiple coal pyrolysis technology, such as internal thermal upright stove, solid heat carrier rapid pyrolysis technology, circular fluid bed and pyrolysis coupling technology, indirect heating pyrolytic technique etc., but, all there is certain shortcoming in the heating process of each technology:
Solid heat carrier rapid pyrolysis technology belongs to typical pyrolytic technique, grows up abroad the earliest, and it is studied and promotes by domestic Dalian University of Technology.Conventional thermal barrier has Ceramic Balls, quartz sand, semicoke etc. Thermal barrier heating main technique is mainly as follows: from reactor coal gas out after purification, then it is transmitted back to hotblast stove combustion, by the flue gas produced, thermal barrier is heated, general by flue gas heat exchange device, fluidized-bed or riser tube heat, so that fine coal is carried out pyrolysis. This heating technique system complex, complicated operation, energy consumption height, heated by gas must waste high heating value gas simultaneously. And adopting half high-temperature flue gas heating, the Cyclone efficiency that flue gas ash is separated with thermal barrier is low, it is easy to cause ash to enter into raw gas.
The most typically vertical heater technology in gas direct heating technology, project is more at home at present. Its main technique is as follows: from vertical heater purified gas out and air, strong redox reaction releases heat occurs, after this heat passes to fine coal, fine coal is heated to 500 DEG C and carries out pyrolysis. After the gas and vapor permeation of flue gas and the pyrolysis generation generated, upwards flow, with fine coal anti-phase and go. In raw gas uphill process, carry out heat exchange with the fine coal of decline, to transfer heat to fine coal. At gas outlet, raw gas temperature is generally about 100 DEG C. This type of furnace throughput is by the restriction of heating process, and coal is heated by the high-temperature flue gas namely produced by purified gas and air, and heating will inevitably be caused uneven, and the caloric power of gas simultaneously produced is low, can not use as industrial chemicals, only can use as low calorie fuels.
Circular fluid bed and pyrolysis coupling system technology have large-scale experiment project, but substantially do not have industrialization promotion. It mainly adopts high-temperature boiler coal ash to be heated by fine coal, high temperature coal ash and fine coal short mix in reactor, and heat transfer, completes pyrolytic reaction. Pyrolysis plant seemingly, but it is generally required to is built in power plant or has near large-scale Fluidized Bed Boiler, restriction technologies popularization by this technology and high-temperature heat carrier technology type.
Chinese patent CN201010153412.0 discloses the method that blue charcoal prepared by a kind of external-heat horizontally-arranged revolution charring furnace thermo-cracking raw coal, and after revolution charring furnace heating adopts purification, coal gas carries out burning in combustion chamber. This technology generates caloric power of gas height, but the high-temperature flue gas produced with high heating value gas heats to revolution charring furnace, less economical.
In a word, all there is certain defect in current pulverized coal pyrolysis technology. Based on this, it is necessary to provide the pulverized coal pyrolysis device that a kind of heat exchange efficiency is higher, equipment simple and economy is higher.
Summary of the invention
The main purpose of the present invention is to provide a kind of pulverized coal pyrolysis device, to solve the problem that high heat exchange efficiency in existing pulverized coal pyrolysis technology, equipment simplification and high economy are difficult to get both.
In order to realize above-mentioned purpose, according to an aspect of the present invention, it provides a kind of pulverized coal pyrolysis device, comprising: rotatable radiation bed, rotatable radiation bed is provided with fine coal opening for feed, thermal medium inlet, thermal medium outlet, semicoke outlet and raw gas venting port; Hotblast stove, hotblast stove is provided with semicoke import and hot blast venting port, and semicoke import is connected with the semicoke outlet in rotatable radiation bed; And flue gas ejector, flue gas ejector is provided with hot blast inlet mouth, draws emanate inlet mouth and injector outlet, hot blast inlet mouth is connected with the hot blast venting port on hotblast stove, injector outlet is connected with the thermal medium inlet in rotatable radiation bed, and draws inlet mouth of emanating and be connected with the thermal medium outlet in rotatable radiation bed.
Further, above-mentioned hotblast stove comprises: combustion chamber, and combustion chamber is provided with burner, lighter for ignition, combustion-supporting wind inlet and semicoke import;And settling pocket, settling pocket and combustion chamber, settling pocket is provided with flue-dust retainer and hot blast venting port.
Further, above-mentioned combustion chamber is connected with the bottom of settling pocket, and hot blast venting port is positioned at the top of settling pocket, and flue-dust retainer is positioned at the bottom of settling pocket; Or combustion chamber is connected with the top of settling pocket, settling pocket is provided with one or more windsheild, between windsheild and the inwall of settling pocket, forms the air-guiding aisle of bending, and hot blast venting port is positioned at the side away from combustion chamber of settling pocket.
Further, above-mentioned settling pocket is provided with multiple windsheild, windsheild has coupling end and free end, multiple windsheild comprises multiple first windsheild on the roof being arranged on settling pocket and is arranged on the diapire of settling pocket second gear wind plate, it is provided with second gear wind plate between two adjacent the first windsheilds, and the first windsheild and second gear wind plate overlap on air current flow direction, so that the air-guiding aisle of bending is W type.
Further, in above-mentioned hotblast stove, the path between combustion chamber and settling pocket is also provided with mixing section, mixing section is provided with and regulates wind inlet mouth.
Further, above-mentioned rotatable radiation bed comprises rotating first housing and is arranged in the radiator tube of the first housing, the import of radiator tube is connected with thermal medium inlet, the outlet of radiator tube is connected with thermal medium outlet, and the outlet of fine coal opening for feed, semicoke and raw gas venting port are all positioned on the first housing.
Further, above-mentioned radiator tube is internal thread seamless tube.
Further, the first housing of above-mentioned rotatable radiation bed comprises feed end and discharge end, and fine coal opening for feed is arranged on feed end, and semicoke outlet and raw gas venting port are all arranged on discharge end, and rotatable radiation bed is obliquely installed downwards along feed end to discharge end.
Further, above-mentioned also comprising waste heat boiler, waste heat boiler comprises: interchanger, and interchanger is provided with heat smoke inlet mouth, cold flue gas venting port, entrance of cooling water and vapour outlet, heat smoke inlet mouth is connected with thermal medium outlet, and inlet mouth of emanating is connected cold flue gas venting port with drawing; And drum, drum is provided with steam inlet, steam inlet is connected with the vapour outlet on interchanger.
Further, above-mentioned interchanger is vertical heat exchanger, and interchanger comprises the 2nd housing and is positioned at the heat transfer tube of the 2nd enclosure interior, and heat transfer tube is provided with entrance of cooling water and vapour outlet; 2nd housing is provided with heat smoke inlet mouth and cold flue gas venting port.
Further, above-mentioned also comprising fly-ash separator, fly-ash separator is provided with cold flue gas inlet mouth, purification wind venting port and second row ash mouth, cold flue gas inlet mouth is connected with cold flue gas venting port, and inlet mouth of emanating is connected purification wind venting port with drawing.
Further, above-mentioned purification wind venting port and draw and be disposed with the first blower fan and the 2nd blower fan on the stream road emanating between inlet mouth, and stream road between the first blower fan and the 2nd blower fan is also provided with exhaust branch.
In pulverized coal pyrolysis device provided by the invention, it is that the semicoke being difficult to process produced by pulverized coal pyrolysis directly burns in hotblast stove, and the high-temperature flue gas that burning produces is back to the heat of rotatable radiation bed supply pulverized coal pyrolysis. Such set-up mode is conducive to making full use of the heat of semicoke, solves the problem that semicoke process is difficult. Simultaneously, flue gas ejector is utilized to draw to be incident upon in rotatable radiation bed by the high-temperature flue gas that coal-char combustion generates and provide heat, can the pressure of circulated gases in overall improved system, thus avoid the dust in high-temperature flue gas to block the hot media channel of rotatable radiation bed, or the problem that the heat exchange efficiency that causes on hot media channel of dust adhesion is poor.What adopt in this flue gas ejector draws the high-temperature flue gas emanated as heat exchange in rotatable radiation bed terminates, can also effectively utilize coal-char combustion heat so further, and utilize heat exchange to terminate the temperature of the high-temperature flue gas that the lower flue gas of rear temperature regulates coal-char combustion to generate, make the thermal medium entering rotatable radiation bed have more suitable temperature. In addition, the equipment of this pulverized coal pyrolysis device is simple, energy-conserving and environment-protective, good economy performance. In a word, the above-mentioned pulverized coal pyrolysis device that Ben Faming provides, its heat exchange efficiency height, equipment is simple and good economy performance, is highly suitable for the pyrolysis processing of fine coal, for realize coal, oil, gas multi-production process create condition.
Accompanying drawing explanation
The Figure of description of the part forming the application is used to provide a further understanding of the present invention, and the schematic description and description of the present invention, for explaining the present invention, does not form inappropriate limitation of the present invention. In the accompanying drawings:
Fig. 1 shows pulverized coal pyrolysis device schematic diagram according to an embodiment of the present;
Fig. 2 shows the structural representation according to hotblast stove in an embodiment of the present invention;
Fig. 3 shows the structural representation according to hotblast stove in the present invention's another kind of embodiment;
Fig. 4 shows the structural representation according to hotblast stove in another embodiment of the present invention; And
Fig. 5 shows the structural representation of the combustion chamber according to hotblast stove in an embodiment of the present invention.
Wherein, above-mentioned accompanying drawing comprises the following drawings mark:
10, rotatable radiation bed; 101, fine coal opening for feed; 102, thermal medium inlet; 103, thermal medium outlet; 104, semicoke outlet; 105, raw gas venting port; 20, hotblast stove; 201, semicoke import; 202, hot blast venting port; 21, combustion chamber; 211, burner; 212, lighter for ignition; 213, combustion-supporting wind inlet; 214, slag-drip opening; 22, settling pocket; 221, flue-dust retainer; 222, windsheild; 30, flue gas ejector; 301, hot blast inlet mouth; 302, inlet mouth of emanating is drawn; 303, injector outlet; 40, waste heat boiler; 401, heat smoke inlet mouth; 402, cold flue gas venting port; 50, fly-ash separator; 501, cold flue gas inlet mouth; 502, wind venting port is purified; 503, second row ash mouth; 11, the first blower fan; 12, the 2nd blower fan.
Embodiment
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually. Below with reference to the accompanying drawings and come the present invention is described in detail in conjunction with the embodiments.
Described by background section, existing pulverized coal pyrolysis technology exists the problem that high heat exchange efficiency, equipment simplification and high economy are difficult to get both. In order to address this problem, the present invention provides a kind of pulverized coal pyrolysis device, and as shown in Figure 1, it comprises rotatable radiation bed 10, hotblast stove 20 and flue gas ejector 30; Rotatable radiation bed 10 is provided with fine coal opening for feed 101, thermal medium inlet 102, thermal medium outlet 103, semicoke outlet 104 and raw gas venting port 105; Being provided with semicoke import 201 and hot blast venting port 202 on hotblast stove 20, semicoke import 201 is connected with the semicoke outlet 104 in rotatable radiation bed 10; Flue gas ejector 30 is provided with hot blast inlet mouth 301, draws emanate inlet mouth 302 and injector outlet 303, hot blast inlet mouth 301 is connected with the hot blast venting port 202 on hotblast stove 20, injector outlet 303 is connected with the thermal medium inlet 102 in rotatable radiation bed 10, and draws inlet mouth 302 of emanating and be connected with the thermal medium outlet 103 in rotatable radiation bed 10.
In above-mentioned pulverized coal pyrolysis device provided by the invention, comprise rotatable radiation bed 10, hotblast stove 20 and flue gas ejector 30. The semicoke that wherein in rotatable radiation bed 10, pulverized coal pyrolysis produces, after semicoke outlet 104 out, enters into hotblast stove 20 and directly carries out coal-char combustion. Coal-char combustion generate high-temperature flue gas flue gas ejector 30 draw the effect of penetrating under, enter the thermal medium inlet 102 of rotatable radiation bed 10 with higher pressure, be fine coal pyrolysis provide heat.
Compared to the complicated procedures of forming of gas recovery of heat of semicoke being gasified, gasifies, gasification gas burning, burning gas supply pyrolysis, in the pulverized coal pyrolysis device that the present invention is above-mentioned, it is that the semicoke being difficult to process produced by pulverized coal pyrolysis directly burns in hotblast stove 20, and the high-temperature flue gas that burning produces is back to the heat that rotatable radiation bed 10 supplies pulverized coal pyrolysis. Such set-up mode is conducive to making full use of the heat of semicoke, solves the problem that semicoke process is difficult. Simultaneously, flue gas ejector 30 is utilized to draw to be incident upon in rotatable radiation bed 10 by the high-temperature flue gas that coal-char combustion generates and provide heat, can the pressure of circulated gases in overall improved system, thus avoid the dust in high-temperature flue gas to block the hot media channel of rotatable radiation bed 10, or the problem that the heat exchange efficiency that causes on hot media channel of dust adhesion is poor. What adopt in this flue gas ejector 30 draws the high-temperature flue gas emanated as heat exchange in rotatable radiation bed 10 terminates, can also effectively utilize coal-char combustion heat so further, and utilize heat exchange to terminate the temperature of the high-temperature flue gas that the lower flue gas of rear temperature regulates coal-char combustion to generate, make the thermal medium entering rotatable radiation bed 10 have more suitable temperature. In addition, the equipment of this pulverized coal pyrolysis device is simple, energy-conserving and environment-protective, good economy performance. In a word, the above-mentioned pulverized coal pyrolysis device that Ben Faming provides, its heat exchange efficiency height, equipment is simple and good economy performance, is highly suitable for the pyrolysis processing of fine coal, for realize coal, oil, gas multi-production process create condition.
Preferably, above-mentioned flue gas ejector 30 is low-pressure injection device, draws below the pressure 20KPa that emanates, and being drawn temperature of emanating is 1350～1500 DEG C, and the flue-gas temperature that injector exports 303 places is down to 800～1000 DEG C. Preferably, the material of flue gas ejector 30 selects high temperature resistant material, or there is heat-resisting antiwear paint inside, outside general steel plate.
The above-mentioned hotblast stove of preferred the present invention 20 is burning below 2mm semicoke foam, or burning semi-coke powder, or the hotblast stove of burning below 25mm powder Jiao. In a kind of preferred embodiment, as shown in Figures 2 and 3, hotblast stove 20 comprises combustion chamber 21 and settling pocket 22; Combustion chamber 21 is provided with burner 211, lighter for ignition 212, combustion-supporting wind inlet 213 and semicoke import 201; Settling pocket 22 is connected with combustion chamber 21, and settling pocket 22 is provided with flue-dust retainer 221 and hot blast venting port 202. Hotblast stove 20 arranges combustion chamber 21, it is possible to for coal-char combustion provides reacting environment. And settling pocket 22 is set, the high-temperature flue gas that coal-char combustion can be made to generate carries out part particles settling before continuing flue gas ejector 30 after entering, remove the particle that in high-temperature flue gas, particle diameter is bigger, thus be conducive to the dustiness in reduction high-temperature flue gas, it is to increase the heat exchange efficiency in rotatable radiation bed 10.
In actual mechanical process, concrete technique can be as follows: below 2mm semicoke is sent in hotblast stove 20 by feed system, and under the effect of burner blower, Thorough combustion, combustion chamber 21 temperature can reach 1350～1500 DEG C.High-temperature flue gas enters settling pocket 22 and carries out thick dedusting, removes by part macrobead dust. The high-temperature flue gas of thick dedusting, under the effect of flue gas ejector 30, draws hotblast stove 20, and the temperature exporting 303 place's high-temperature flue gas at injector is down to 800～1000 DEG C.
Flue gas after temperature adjustment flue gas ejector 30 draw the effect of penetrating under enter in rotatable radiation bed 10, to fine coal conduct heat so that it completes pyrolytic reaction. When rotatable radiation bed 10 is rotated, fine coal moves forward in kiln, with the high-temperature flue gas heat exchange gradually from hotblast stove 20 in moving process, the gradual temperature of fine coal raises, until when coal is heated to 500～550 DEG C, fine coal completes pyrolytic reaction and generates the semicoke of 550～630 DEG C and the raw gas (comprising tar steam and coal gas) of about 500 DEG C, and raw gas is from the outflow suitable for reading of kiln tail, and high-temperature semi-coke falls from lower mouth.
In a kind of preferred embodiment, as shown in Figure 2, combustion chamber 21 is connected with the bottom of settling pocket 22, and hot blast venting port 202 is positioned at the top of settling pocket 22, and flue-dust retainer 221 is positioned at the bottom of settling pocket 22. In such horizontal hot air furnace, the high-temperature flue gas produced from combustion chamber 21 can enter from the bottom of settling pocket 22, upwards moves to the hot blast venting port 202 at settling pocket 22 top in rotation direction. In the process that rotation direction is upwards run, the macrobead in high-temperature flue gas can more easily fall such that it is able to improves the purification rate of high-temperature flue gas further. Or, as shown in Figure 3 and Figure 4, combustion chamber 21 is connected with the top of settling pocket 22, settling pocket 22 is provided with one or more windsheild 222, the air-guiding aisle of bending is formed, and hot blast venting port 202 is positioned at the side away from combustion chamber 21 of settling pocket 22 between the inwall of windsheild 222 and settling pocket 22. In such set-up mode, utilize the air-guiding aisle forming bending between the inwall of windsheild 222 and settling pocket 22, the high-temperature flue gas song in settling pocket 22 produced in combustion chamber 21 can be made to be forwarded to hot blast venting port 202, song march forward and windsheild 222 barrier effect under, the macrobead in high-temperature flue gas is more conducive to making to settle down, with the dustiness reduced further in flue gas, it is to increase the heat exchange efficiency of follow-up rotatable radiation bed 10.
In a kind of preferred embodiment, as shown in Figure 4, settling pocket 22 is provided with multiple windsheild 222, windsheild 222 has coupling end and free end, multiple windsheild 222 comprises multiple first windsheild on the roof being arranged on settling pocket 22 and is arranged on the diapire of settling pocket 22 second gear wind plate, it is provided with second gear wind plate, and the first windsheild and second gear wind plate overlap on air current flow direction, so that the air-guiding aisle of bending is W type between two adjacent the first windsheilds. Such set-up mode can reduce the dustiness in high-temperature flue gas further, it is to increase the heat exchange efficiency of follow-up rotatable radiation bed 10. In a preferred embodiment, as shown in Figure 4, it is possible to chain row is set below the semicoke import 201 in combustion chamber 21, to accept in semicoke import 201 semicoke entered, thus improves the rate of combustion of semicoke. More preferably, the hotblast stove shown in Fig. 4 is burnt for below the 25mm powder that burns, and the hotblast stove shown in Fig. 2 and Fig. 3 is for the burnt foam of below the 2mm that burns or burnt powder.
In a kind of preferred embodiment, in hotblast stove 20, the path between combustion chamber 21 and settling pocket 22 is also provided with mixing section, mixing section is provided with and regulates wind inlet mouth. Path between combustion chamber 21 and settling pocket 22 arranges mixing section, high-temperature flue gas can be made to mix with the adjustment wind regulating wind inlet mouth to enter, to adjust the temperature of high-temperature flue gas and the oxygen level (its oxygen level can be made lower than 5%) of the inside that burning generates, thus improve the security of equipment further.
In a kind of preferred embodiment, the bottom of combustion chamber 21 is provided with one or more slag-drip opening 214, is provided with one or more first ash discharging hole bottom the flue-dust retainer 221 of settling pocket 22.
In addition, combustion chamber 21 can arrange multiple burner 211 and the multiple lighter for ignitions 212 mated mutually with it, combustion-supporting wind inlet 213 and semicoke import 201. And the distribution of multiple burner 211 can be different directions, such as can along the radial array of combustion chamber 21 or axial array. The flame of concrete burner 211 is towards adjusting, and such as radial flame burning or tangential flame as shown in Figure 5 are burnt.
In a kind of preferred embodiment, rotatable radiation bed 10 comprises rotating first housing and is arranged in the radiator tube of the first housing, the import of radiator tube is connected with thermal medium inlet 102, the outlet of radiator tube is connected with thermal medium outlet 103, and fine coal opening for feed 101, semicoke outlet 104 and raw gas venting port 105 are all positioned on the first housing. Utilizing this rotatable radiation bed 10 to carry out pulverized coal pyrolysis, high-temperature flue gas walks radiator tube inside, and first enclosure interior of fine coal outside radiator tube is indirect heating. Utilizing radiator tube to carry out indirect heating, especially many group radiator tubes carry out indirect heating, it is possible to making fine coal pyrolysis more fully, the caloric power of gas height of generation, semicoke steady quality, tar taste is higher. Concrete radiator tube set-up mode can be utilize the rforated plate bracing of kiln head and kiln tail to arrange.
In a kind of preferred embodiment, radiator tube is internal thread seamless tube. Internal thread seamless tube selected by radiator tube, can not only increase heat interchanging area, but also can increase the coefficient of heat transfer, is conducive to improving further heat exchange efficiency, and reduces facility investment.
In a kind of preferred embodiment, first housing of rotatable radiation bed 10 comprises feed end and discharge end, fine coal opening for feed 101 is arranged on feed end, and semicoke outlet 104 and raw gas venting port 105 are all arranged on discharge end, and rotatable radiation bed 10 is obliquely installed downwards along feed end to discharge end. Such set-up mode more is conducive to making the abundant pyrolysis of fine coal. Preferably, feed end is 1～5 ° to the obliquity of discharge end.
In a kind of preferred embodiment, also comprising waste heat boiler 40 in above-mentioned pulverized coal pyrolysis device, this waste heat boiler 40 comprises interchanger and drum; Being provided with heat smoke inlet mouth 401, cold flue gas venting port 402, entrance of cooling water and vapour outlet on interchanger, heat smoke inlet mouth 401 is connected with thermal medium outlet 103, and inlet mouth 302 of emanating is connected cold flue gas venting port 402 with drawing; Being provided with steam inlet on drum, steam inlet is connected with the vapour outlet on interchanger. Adopt the heat in waste heat boiler 40 recovered flue gas, it is steam by converting heat, both can project use by oneself, it is also possible to generating, it is to increase system thermal efficiency utilizes.
In a kind of preferred embodiment, interchanger is vertical heat exchanger, and interchanger comprises the 2nd housing and is positioned at the heat transfer tube of the 2nd enclosure interior, and heat transfer tube is provided with entrance of cooling water and vapour outlet; 2nd housing is provided with heat smoke inlet mouth 401 and described cold flue gas venting port 402. This interchanger adopts partition tubular type heat transfer tube and forces water cycle principle of work, and water coolant adopts soft water, and water coolant enters in heat transfer tube by the 2nd housing bottom, and by the gas converting heat of the outer flowing of tube wall and pipe, the steam of generation enters drum.
In a kind of preferred embodiment, interchanger also comprises ash back-blowing device clearly, and clear ash back-blowing device is provided with blowback air venting port;Also being provided with blowback air inlet mouth on heat transfer tube, blowback air inlet mouth is connected with blowback air venting port. Carry ash back-blowing device clearly, it is possible to the inside of intermittent exchange heat pipe carries out reverse blowing disposal, to prevent heat transfer tube blocking. Specifically, clear ash back-blowing device can be high pressure gas back-blowing device or acoustic wave soot blower. Utilizing high pressure gas back-blowing device regularly high pressure gas to be drawn is incident upon in heat transfer tube, and after high pressure gas discharges, the ash in pipe is impacted by expansion generation air-flow. Adopt acoustic wave soot blower, it is possible to multiple acoustic wave soot blower is set at blowback air inlet port top, regularly opens, remove by the dust in pipe.
In a kind of preferred embodiment, above-mentioned pulverized coal pyrolysis device also comprises fly-ash separator 50, this fly-ash separator 50 is provided with cold flue gas inlet mouth 501, purification wind venting port 502 and second row ash mouth 503, cold flue gas inlet mouth 501 is connected with cold flue gas venting port 402, and inlet mouth 302 of emanating is connected purification wind venting port 502 with drawing. Fly-ash separator 50 is set, it is possible to the high-temperature flue gas completing heat exchange from rotatable radiation bed 10 is carried out purifying treatment, reduces its ash content. And the flue that ash content is lower subsequently is emanated as high-temperature flue gas out in hotblast stove 20 provides power as drawing again, mix with it. This makes it possible to reduce further the ash content of the flue gas entering rotatable radiation bed 10, thus improve its heat exchange efficiency further.
In a kind of preferred embodiment, fly-ash separator 50 is sack cleaner. The efficiency of dust collection of sack cleaner is higher, it is possible to reduce the dustiness in high-temperature flue gas further, it is to increase the heat exchange efficiency of rotatable radiation bed 10. Preferably, the filtrate heatproof more than 1300 DEG C in grain bed fly-ash separator or too cotton filter collector, makes the dustiness of the high-temperature flue gas after purification lower than 30mg/Nm3。
In a kind of preferred embodiment, purification wind venting port 502 and draw and be disposed with the first blower fan 11 and the 2nd blower fan 12 on the stream road emanated between inlet mouth 302, and stream road between the first blower fan 11 and the 2nd blower fan 12 is also provided with exhaust branch.
In the operating process of reality, 250 DEG C-350 DEG C can be down to from the thermal medium outlet 103 of rotatable radiation bed 10 flue-gas temperature out. Under the effect of the first blower fan 11, enter into the interchanger of waste heat boiler 40. Wherein flue gas is walked outside heat transfer tube, and water coolant is walked in pipe, carries out reverse row heat exchange, and the steam of generation enters in drum. Flue gas is cooled to about 160 DEG C from 250-350 DEG C, then enters in fly-ash separator 50, flows in bag at filter bag outer wall, is got off by dust-filtering by filter bag in flow process, and the ash under filter is discharged from second row ash mouth 503. Part enters in the 2nd blower fan 12 from fly-ash separator 50 flue gas out, is sent in flue gas ejector 30 as drawing to emanate under the effect of the 2nd blower fan 12, draws and mixes with high-temperature flue gas after having penetrated. Other partial fume purifies discharge from exhaust branch.
Preferably, the 2nd blower fan 12 is horizontal structure, and flue gas is delivered in flue gas ejector 30 by blower fan heatproof 150～250 DEG C, as drawing the power gas penetrating high-temperature flue gas.
From above description, can find out, the above embodiments of the present invention achieve following technique effect: in pulverized coal pyrolysis device provided by the invention, it is that the semicoke being difficult to process produced by pulverized coal pyrolysis directly burns in hotblast stove, and the high-temperature flue gas that burning produces is returned the heat of rotatable radiation bed supply pulverized coal pyrolysis. Such set-up mode is conducive to making full use of the heat of semicoke, solves the problem that semicoke process is difficult. Simultaneously, flue gas ejector is utilized to draw to be incident upon in rotatable radiation bed by the high-temperature flue gas that coal-char combustion generates and provide heat, can the pressure of circulated gases in overall improved system, thus avoid the dust in high-temperature flue gas to block the hot media channel of rotatable radiation bed, or the problem that the heat exchange efficiency that causes on hot media channel of dust adhesion is poor. What adopt in this flue gas ejector draws the high-temperature flue gas emanated as heat exchange in rotatable radiation bed terminates, can also effectively utilize coal-char combustion heat so further, and utilize heat exchange to terminate the temperature of the high-temperature flue gas that the lower flue gas of rear temperature regulates coal-char combustion to generate, make the thermal medium entering rotatable radiation bed have more suitable temperature. In addition, the equipment of this pulverized coal pyrolysis device is simple, energy-conserving and environment-protective, good economy performance. In a word, the above-mentioned pulverized coal pyrolysis device that Ben Faming provides, its heat exchange efficiency height, equipment is simple and good economy performance, is highly suitable for the pyrolysis processing of fine coal, for realize coal, oil, gas multi-production process create condition.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment of doing, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (12)
1. a pulverized coal pyrolysis device, it is characterised in that, comprising:
Rotatable radiation bed (10), described rotatable radiation bed (10) is provided with fine coal opening for feed (101), thermal medium inlet (102), thermal medium outlet (103), semicoke outlet (104) and raw gas venting port (105);
Hotblast stove (20), being provided with semicoke import (201) and hot blast venting port (202) on described hotblast stove (20), described semicoke import (201) is connected with described semicoke outlet (104) on described rotatable radiation bed (10); And
Flue gas ejector (30), described flue gas ejector (30) is provided with hot blast inlet mouth (301), draw inlet mouth of emanating (302) and injector outlet (303), described hot blast inlet mouth (301) is connected with the described hot blast venting port (202) on described hotblast stove (20), described injector outlet (303) is connected with the described thermal medium inlet (102) on described rotatable radiation bed (10), and described in draw inlet mouth of emanating (302) and be connected with the described thermal medium outlet (103) on described rotatable radiation bed (10).
2. pulverized coal pyrolysis device according to claim 1, it is characterised in that, described hotblast stove (20) comprising:
Combustion chamber (21), described combustion chamber (21) are provided with burner (211), lighter for ignition (212), combustion-supporting wind inlet (213) and described semicoke import (201); And
Settling pocket (22), described settling pocket (22) is connected with described combustion chamber (21), and described settling pocket (22) is provided with flue-dust retainer (221) and described hot blast venting port (202).
3. pulverized coal pyrolysis device according to claim 2, it is characterised in that,
Described combustion chamber (21) is connected with the bottom of described settling pocket (22), and described hot blast venting port (202) is positioned at the top of described settling pocket (22), described flue-dust retainer (221) is positioned at the bottom of described settling pocket (22); Or
Described combustion chamber (21) is connected with the top of described settling pocket (22), described settling pocket (22) is provided with one or more windsheild (222), the air-guiding aisle of bending is formed, and described hot blast venting port (202) is positioned at the side away from described combustion chamber (21) of described settling pocket (22) between the inwall of described windsheild (222) and described settling pocket (22).
4. pulverized coal pyrolysis device according to claim 3, it is characterized in that, described settling pocket (22) is provided with multiple described windsheild (222), described windsheild (222) has coupling end and free end, multiple described windsheild (222) comprises multiple first windsheild on the roof being arranged on described settling pocket (22) and is arranged on the diapire of described settling pocket (22) second gear wind plate, described second gear wind plate it is provided with between described first windsheild of adjacent two, and described first windsheild and described second gear wind plate overlap on air current flow direction, so that the air-guiding aisle of described bending is W type.
5. pulverized coal pyrolysis device according to claim 2, it is characterized in that, in described hotblast stove (20), the path between described combustion chamber (21) and described settling pocket (22) is also provided with mixing section, described mixing section is provided with and regulates wind inlet mouth.
6. pulverized coal pyrolysis device according to any one of claim 1 to 5, it is characterized in that, described rotatable radiation bed (10) comprises rotating first housing and is arranged in the radiator tube of described first housing, the import of described radiator tube is connected with described thermal medium inlet (102), the outlet of described radiator tube is connected with described thermal medium outlet (103), and described fine coal opening for feed (101), described semicoke outlet (104) and described raw gas venting port (105) are all positioned on described first housing.
7. pulverized coal pyrolysis device according to claim 6, it is characterised in that, described radiator tube is internal thread seamless tube.
8. pulverized coal pyrolysis device according to claim 6, it is characterized in that, described first housing of described rotatable radiation bed (10) comprises feed end and discharge end, described fine coal opening for feed (101) is arranged on described feed end, described semicoke outlet (104) and described raw gas venting port (105) are all arranged on described discharge end, and described rotatable radiation bed (10) is obliquely installed downwards along described feed end to described discharge end.
9. pulverized coal pyrolysis device according to any one of claim 1 to 5, it is characterised in that, also comprise waste heat boiler (40), described waste heat boiler (40) comprising:
Interchanger, described interchanger is provided with heat smoke inlet mouth (401), cold flue gas venting port (402), entrance of cooling water and vapour outlet, described heat smoke inlet mouth (401) is connected with described thermal medium outlet (103), and described cold flue gas venting port (402) is connected with the described inlet mouth of emanating (302) that draws; And
Drum, described drum is provided with steam inlet, and described steam inlet is connected with the described vapour outlet on described interchanger.
10. pulverized coal pyrolysis device according to claim 9, it is characterized in that, described interchanger is vertical heat exchanger, and described interchanger comprises the 2nd housing and is positioned at the heat transfer tube of described 2nd enclosure interior, and described heat transfer tube is provided with described entrance of cooling water and described vapour outlet; Described 2nd housing is provided with described heat smoke inlet mouth (401) and described cold flue gas venting port (402).
11. pulverized coal pyrolysis devices according to claim 9, it is characterized in that, also comprise fly-ash separator (50), described fly-ash separator is provided with cold flue gas inlet mouth (501), purification wind venting port (502) and second row ash mouth (503), described cold flue gas inlet mouth (501) is connected with described cold flue gas venting port (402), and described purification wind venting port (502) is connected with the described inlet mouth of emanating (302) that draws.
12. pulverized coal pyrolysis devices according to claim 11, it is characterized in that, described purification wind venting port (502) and the described stream road drawn between inlet mouth of emanating (302) are disposed with the first blower fan (11) and the 2nd blower fan (12), and stream road between described first blower fan (11) and described 2nd blower fan (12) is also provided with exhaust branch.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610193143.8A CN105670664B (en) | 2016-03-29 | 2016-03-29 | Pulverized coal pyrolysis device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610193143.8A CN105670664B (en) | 2016-03-29 | 2016-03-29 | Pulverized coal pyrolysis device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105670664A true CN105670664A (en) | 2016-06-15 |
| CN105670664B CN105670664B (en) | 2019-07-09 |
Family
ID=56224759
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610193143.8A Active CN105670664B (en) | 2016-03-29 | 2016-03-29 | Pulverized coal pyrolysis device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105670664B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950198A (en) * | 2016-06-22 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Powder coal pyrolysis dedusting system with built-in circulating granular bed |
| CN109468139A (en) * | 2018-10-29 | 2019-03-15 | 合肥工业大学 | A kind of biomass graded pyrolysis and combustion device |
| CN114806614A (en) * | 2022-04-08 | 2022-07-29 | 浙江工业大学 | Rotary kiln pyrolysis carbonization device and process based on smoke injection recycling |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063593A (en) * | 2006-04-26 | 2007-10-31 | 霍镰泉 | Method for reducing coal consumption of hot-air stove |
| CN104033889A (en) * | 2014-05-28 | 2014-09-10 | 山东科技大学 | Heat accumulating type biomass gasification combustion device and production process thereof |
| CN105331377A (en) * | 2015-11-16 | 2016-02-17 | 北京神雾环境能源科技集团股份有限公司 | Coal pyrolysis method and system |
| CN205653408U (en) * | 2016-03-29 | 2016-10-19 | 新疆广汇中化能源技术开发有限公司 | Powder coal pyrolysis device |
-
2016
- 2016-03-29 CN CN201610193143.8A patent/CN105670664B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063593A (en) * | 2006-04-26 | 2007-10-31 | 霍镰泉 | Method for reducing coal consumption of hot-air stove |
| CN104033889A (en) * | 2014-05-28 | 2014-09-10 | 山东科技大学 | Heat accumulating type biomass gasification combustion device and production process thereof |
| CN105331377A (en) * | 2015-11-16 | 2016-02-17 | 北京神雾环境能源科技集团股份有限公司 | Coal pyrolysis method and system |
| CN205653408U (en) * | 2016-03-29 | 2016-10-19 | 新疆广汇中化能源技术开发有限公司 | Powder coal pyrolysis device |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950198A (en) * | 2016-06-22 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Powder coal pyrolysis dedusting system with built-in circulating granular bed |
| CN109468139A (en) * | 2018-10-29 | 2019-03-15 | 合肥工业大学 | A kind of biomass graded pyrolysis and combustion device |
| CN109468139B (en) * | 2018-10-29 | 2020-11-06 | 合肥工业大学 | Biomass staged pyrolysis combustor |
| CN114806614A (en) * | 2022-04-08 | 2022-07-29 | 浙江工业大学 | Rotary kiln pyrolysis carbonization device and process based on smoke injection recycling |
| CN114806614B (en) * | 2022-04-08 | 2024-01-16 | 浙江工业大学 | Rotary kiln pyrolysis carbonization device and process based on smoke injection recycling |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105670664B (en) | 2019-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104629807A (en) | Chilling process gasifier with high-temperature heat recovery unit | |
| CN105062528B (en) | A kind of pyrolysis of coal multi-production process and its device suitable for coal-powder boiler | |
| CN103992824A (en) | Double-cyclone coal pyrolysis gasification step converting device and double-cyclone coal pyrolysis gasification step converting method | |
| CN103740409B (en) | Multi-stage gas distribution high-temperature coal gasification device and method | |
| CN105623689A (en) | Coal pyrolysis system | |
| CN102352262A (en) | Circulated coal gas heat carrier fluidized bed ash coal pyrolysis device and method | |
| CN204550484U (en) | A kind of chilling process vapourizing furnace with high-temperature hot retrieving arrangement | |
| CN103980912A (en) | Destructive distillation method and device for brown coal | |
| CN105670664A (en) | Pulverized coal pyrolysis device | |
| CN106224972A (en) | The refuse gasification combustion gas of high-moisture gas recycling and steam turbine combined generating system | |
| CN205860025U (en) | Collect the dry distilling of organic particulate matter, gasify the dry-distillation incineration stove with burning one | |
| CN206033675U (en) | Low tar gas device of dry distillation of jointly gasifying preparation | |
| RU169609U1 (en) | Installation for producing synthesis gas from coal-water fuel | |
| CN202246560U (en) | Fluidized bed pulverized coal pyrolyzation device taking cycling coal gas heat as carrier | |
| CN105670665B (en) | Pulverized coal pyrolysis device | |
| CN106978215A (en) | A kind of two-stage type biomass pyrolytic gasification revolving bed and pyrolysis gasification method | |
| CN218434919U (en) | Fluidization pyrolysis activation integrated device for preparing activated carbon by physical method | |
| CN205653407U (en) | Coal pyrolysis system | |
| CN205653408U (en) | Powder coal pyrolysis device | |
| CN102260538B (en) | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass | |
| CN205653409U (en) | Powder coal pyrolysis device | |
| CN105925289B (en) | A kind of combined vaporizing destructive distillation prepares low tar gas combustion apparatus | |
| CN205690388U (en) | A kind of high volatile carbon-containing fuel hot efflorescence high efficient combustion device | |
| CN204824727U (en) | Pyrolysis process units based on high temperature mixture in circulating fluidized bed boiler furnace | |
| CN210176801U (en) | Entrained flow bed and circulating fluidized bed combined gasification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20180130 Address after: 839303 the Xinjiang Uygur Autonomous Region Hami Yiwu County NOM town Xingye Road No. 1 Applicant after: Xinjiang Guanghui coal cleaning and refining Co., Ltd. Address before: 830001 the Xinjiang Uygur Autonomous Region economic and Technological Development Zone, Songshan street, No., R & D building, room 871, room 229 Applicant before: XINJIANG GUANGHUI SINOCHEM ENERGY TECHNOLOGY DEVELOPMENT CO., LTD. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |