CN103409156B - Heat carrier destructive distillation system for coal and method thereof - Google Patents
Heat carrier destructive distillation system for coal and method thereof Download PDFInfo
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- CN103409156B CN103409156B CN201310333329.5A CN201310333329A CN103409156B CN 103409156 B CN103409156 B CN 103409156B CN 201310333329 A CN201310333329 A CN 201310333329A CN 103409156 B CN103409156 B CN 103409156B
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Abstract
The invention relates to a heat carrier destructive distillation system for coal, which comprises a raw coal cabin, a flash dryer, and a circulating fluidized bed air heating furnace, wherein a spiral metering conveyor I is arranged at the bottom of the raw coal cabin; a flash dryer is connected with a drying primary separator and an air heating furnace twice cyclone separator; the drying primary separator is connected with a drying secondary separator and a mixer; the air heating furnace twice cyclone separator is connected with a cooling paddle machine and a waste heat boiler; the waste heat boiler is connected with an air heating furnace once cyclone separator connected with the mixer and the circulating fluidized bed air heating furnace; the mixer is connected with an internal thermal rotary gas retort; a separator is connected with a cooling tower and a fluidized bed grading cooler; the cooling tower is connected with a coal gas air blower and a tar oil cooler; the fluidized bed grading cooler is connected with a semi-coke delivery pipe, the drying secondary separator and a grading cyclone separator; the circulating fluidized bed air heating furnace is connected with the grading cyclone separator. In addition, the invention further discloses an application method of the system. The heat carrier destructive distillation system is low in investment and easy to implement, and has high overall efficiency and excellent safety.
Description
Technical field
The present invention relates to coal resources and fully rationally utilize technical field, relate in particular to a kind of thermal barrier distillation system and method thereof of coal.
Background technology
Coal carbonization (pyrolysis) process for upgrading is a lot, and its retort process is endothermic process, according to the difference of heat-supplying mode, can be divided into external-heat and internal heat type.According to the difference of heat-transfer medium, internal heat type can be divided into gaseous heat-carrier method and solid heat carrier method again.
Gaseous heat-carrier method is to adopt high temperature inert gas as destructive distillation thermal source, the ENCOAL technique of the U.S. and CODE technique etc. are gaseous heat-carrier method for destructive distillation, but the method shortcoming is the diluting effect of rare gas element, reduced the quality of coal gas, the particle diameter of feed coal is generally larger simultaneously, and the destructive distillation time needing is long.
Solid heat carrier method is to utilize the sensible heat of high-temp solid that coal is heated, and the particle diameter of the method general requirement coal is crushed in 25mm, has increased like this contact area with solid thermal carriers, and the destructive distillation time is short; Also can avoid the coal gas producing to be diluted, the quality of coal gas is high, and quality of coke tar is good; , by literature research, shown, solid heat carrier method can be fixed in sulphur in ash, effectively reduces the release of sulphur in pyrolytic process meanwhile, and the sulphur content in coal gas is low.
Solid thermal carriers are different according to source, can be divided into two classes: a class is Ceramic Balls, and another kind of is Pyrolysis Char and combustion heat ash.Adopting Ceramic Balls shortcoming is to need extra fuel to its heat supply, and overall thermo-efficiency is lower.Patent (the ZL200710055610.1 of Northeast Electric Power University's application, ZL201220606884.) adopt circulating fluid bed hot-air furnace cycling hot ash and burning ashes as solid thermal carriers, these two patents are more suitable for the pyrolysis of resinous shale, and be not suitable for the pyrolysis of coal, while adopting method that these two patents provide for the pyrolysis of coal, can not get high-quality semicoke product, the semicoke product obtaining is the cinder that burnt or the mixture of semicoke and lime-ash, its calorific value is low and do not have a utility value, and energy consumption is high, there is complete hidden danger in system.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of thermal barrier distillation system little, easy to implement, coal that security is good of investing.
Another technical problem to be solved by this invention is to provide a kind of application method of thermal barrier distillation system of coal of effective reduction energy consumption.
For addressing the above problem, the thermal barrier distillation system of a kind of coal of the present invention, comprise run coal bin, pneumatic dryer, circulating fluid bed hot-air furnace, it is characterized in that: described run coal bin bottom is provided with spiral metering conveyor I, and this spiral metering conveyor I is connected with described pneumatic dryer by blocking valve I; The top of described pneumatic dryer is connected with dry primary separator by pipeline I, and one side is connected with hotblast stove secondary cyclone separator by pipeline II; The top of described dry primary separator is connected with dry second-stage separator by pipeline III, and its bottom is connected with mixing tank; The bottom of described hotblast stove secondary cyclone separator is provided with cooling blade machine, and one side is connected with waste heat boiler by pipeline IV; The top of described cooling blade machine is provided with and cools back the mouth of a river, and its bottom is respectively equipped with cooling filling pipe end, blocking valve II, and this blocking valve II is connected with ash content delivery pipe; The top of described waste heat boiler is provided with superheated vapour discharge outlet, and its bottom is provided with oiler feed mouth, and one side is connected with cyclonic separator of hotblast stove; The bottom of a cyclonic separator of described hotblast stove is connected with described mixing tank, and one side is connected with the top of described circulating fluid bed hot-air furnace by pipeline V; Described mixing tank bottom is provided with interior hot rotary type gas retort, and one end of this interior hot rotary type gas retort is connected with separator; The top of described separator is connected with cooling tower by pipeline VI, and its bottom is connected with fluidized bed classification water cooler; The top of described cooling tower is provided with the coal gas discharge outlet being connected with gas fan, and its bottom is provided with tar emission mouth, and this tar emission mouth is connected with tar emission pipe, tar cooler successively by recycle pump; Described tar cooler is connected with a side roof part of described cooling tower; One side bottom of described fluidized bed classification water cooler is connected with semicoke output tube by blocking valve III, the bottom of its opposite side is connected with the top of described dry second-stage separator through pipeline VII by water cooler recirculation blower, and the top of its opposite side is connected with classification cyclonic separator; In described pipeline VII, by discharge blower fan, be connected with chimney; The top of described classification cyclonic separator is connected with a side of described circulating fluid bed hot-air furnace respectively with bottom; The bottom of described circulating fluid bed hot-air furnace is connected with air input tube by burner blower, and its opposite side is provided with coal dust input aperture, raw coal input aperture, lime-ash discharge outlet, flue gas input aperture from top to bottom successively; Described coal dust input aperture is connected with respectively blocking valve V, conveying fan by Venturi handling machinery, and this blocking valve V is connected with the bottom of described dry second-stage separator; Described raw coal input aperture is connected with spiral metering conveyor II by input channel through blocking valve IV, and this spiral metering conveyor II is connected with described run coal bin; Described flue gas input aperture is connected with described pipeline VII by hotblast stove recirculation blower.
Described interior hot rotary type gas retort refers to lined revolving drum stove.
Described mixing tank is bin type mixing tank.
Described cooling tower refers to a kind of in packing tower, tray column or spray column.
Described tar cooler is shell and tube heat exchanger.
Described pneumatic dryer refers to a kind of in impulse pneumatic drying pipe, straight pipe type airflow drying tube, single hose airflow drying tube, Multi-tube airflow drying tube.
Described dry primary separator is decanter type separator or cyclonic separator.
Described dry second-stage separator refers to a kind of in cyclonic separator, sack cleaner or electric precipitator.
The application method of the thermal barrier distillation system of a kind of coal as above, comprises the following steps:
(1) moisture is greater than after 15% be crushed to≤20mm of raw coal, send in run coal bin, and send in pneumatic dryer by spiral metering conveyor I, blocking valve I, simultaneously, temperature after waste heat boiler recovery part heat is that dedusting is separated again through hotblast stove secondary cyclone separator for 300 ~ 800 ℃ of flue gases, this 300 ~ 800 flue gas enters that in described pneumatic dryer, to carry out the dehydration of coal predrying, obtains respectively moisture content and be 1 ~ 8% coal dust and dried tail gas A after 2 ~ 5s;
(2) the coal dust that described moisture content is 1 ~ 8% and described dried tail gas A together send in dry primary separator and carry out gas solid separation, obtain respectively coal dust and 90 ~ 150 ℃ of flue gases after separation; Coal dust after described separation falls into mixing tank; The dedusting of described 90 ~ 150 ℃ of flue gas drying second-stage separators, obtains respectively the coal dust of dried tail gas B and particle diameter < 0.5mm; Described dried tail gas B discharges from described dry second-stage separator top, and wherein a part drains into chimney by discharge blower fan, and rest part sends into respectively hotblast stove recirculation blower and water cooler recirculation blower recycles; The coal dust of described particle diameter < 0.5mm is sent back in circulating fluid bed hot-air furnace and is burned by Venturi handling machinery;
(3) the described raw coal in described run coal bin is sent into by circulating fluid bed hot-air furnace bottom through spiral metering conveyor II, blocking valve IV, simultaneously, air through burner blower input is sent into by described circulating fluid bed hot-air furnace bottom, the air of conveying fan input is sent into by described circulating fluid bed hot-air furnace top through Venturi handling machinery, and the described dried tail gas B of the part that (2) described step obtains is sent into by described circulating fluid bed hot-air furnace bottom through hotblast stove recirculation blower, burn in the lump with described separated solid phase; Obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash and lime-ash; Described lime-ash is discharged through lime-ash discharge outlet;
(4) described 800 ~ 1100 ℃ of flue gases and described 800 ~ 1100 ℃ of circulating ash are discharged and to be entered cyclonic separator of described hotblast stove and carry out gas solid separation by described circulating fluid bed hot-air furnace top, obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash;
(5) described 800 ~ 1100 ℃ of circulating ash enter in described mixing tank, (2) obtain with described step separated after coal dust in the ratio of coal dust: circulating ash=1kg:1.8kg ~ 2.5kg, tentatively mix, obtain mixture; Described mixture enters interior hot rotary type gas retort by described mixing tank, this interior hot rotary type gas retort is done turning motion under motor drives, make mixture obtain sufficient mixed heat transfer, when being heated to 450 ~ 600 ℃, coal dust there is pyrogenation and carbonization reaction, after 5 ~ 60min, obtain respectively pyrolysis product, i.e. coal gas, tar and semicoke;
After the described interior hot rotary type gas retort of described pyrolysis product discharge, enter separator and carry out gas solid separation, obtain respectively gaseous products and solid phase product; Described gaseous products is sent into cooling tower by described separator top and is carried out oil gas refrigerated separation, obtains respectively coal gas and tar; Described solid phase product is sent in fluidized bed classification water cooler by described separator bottom;
(6) the described dried tail gas B of part that (2) described step obtains passes into from described fluidized bed classification water cooler bottom by water cooler recirculation blower, (5) it is cooling that the solid phase product obtaining with described step carries out fluidisation, obtains respectively semicoke product, the semicoke of granularity < 1mm and the mixture of circulating ash of granularity > 1mm; The semicoke product of described granularity > 1mm is discharged by blocking valve III continuously by described fluidized bed classification water cooler bottom;
(7) the semicoke of described granularity < 1mm and the mixture of circulating ash are discharged and to be entered classification cyclonic separator and carry out gas solid separation by described fluidized bed classification water cooler top under the effect of described dried tail gas B, obtain respectively separated gas phase and separated solid phase; The gas phase of described separation is entered by the middle part of circulating fluid bed hot-air furnace; The solid of described separation is entered as circulating fuel by described circulating fluid bed hot-air furnace bottom;
(8) described 800 ~ 1100 ℃ of flue gases are sent into heating boiler water in described waste heat boiler and are reclaimed heat, and the flue gas after heat exchange, through the further dedusting of described hotblast stove secondary cyclone separator, obtains respectively ash content and dried tail gas C;
Described ash content is discharged system by cooling blade machine through blocking valve II, as the building materials raw material use of Building Materials Factory;
Described dried tail gas C sends into described pneumatic dryer and after described dry primary separator separation, sends into further dedusting in dry second-stage separator, obtains respectively the coal dust of dried tail gas D and particle diameter < 0.5mm; Described dried tail gas D discharges from described dry second-stage separator top, and wherein a part drains into chimney by described discharge blower fan, and rest part sends into respectively described hotblast stove recirculation blower and described water cooler recirculation blower recycles; The coal dust of described particle diameter < 0.5mm is sent back in described circulating fluid bed hot-air furnace and is burned by described Venturi handling machinery.
The present invention compared with prior art has the following advantages:
1, the present invention reclaims the inertia flue gas of 300 ~ 800 ℃ after heat by waste heat boiler and sends in pneumatic dryer as the predrying coal dust of thermal source, and not only the oxygen level of dehumidification system is low, dehumidification system is safe and reliable, and has further improved heat utilization ratio; The coal dust of simultaneously deviating from most of water carries out the load that pyrolysis can reduce gas retort again, thereby effectively reduces the scale of destructive distillation time and gas retort.
2, the present invention is usingd circulating ash and at interior hot rotary type gas retort, is mixed with coal as solid thermal carriers, and not only residence time of material is short, and dry distillation efficiency is high, and can produce high-quality coal gas, tar and semicoke.
3, fluidized bed classification water cooler of the present invention is except by the reuse of semicoke cooling heat, also separated with circulating ash by semicoke, and the semicoke ash content obtaining is low, and calorific value is high, and particle diameter is convenient to greatly transportation and is stored.
4, mainly the burn semicoke of granularity < (1 ~ 3) mm and from the former coal dust of granularity < 0.5mm of pneumatic dryer of circulating fluid bed hot-air furnace of the present invention, two kinds of raw materials add at the different sites of circulating fluid bed hot-air furnace, sufficient combustion, stable.
5, the present invention invests little, easy to implement and overall efficiency is high, both can be used for the pyrogenation and carbonization of coal, also can be used for the pyrogenation and carbonization of resinous shale.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
Fig. 1 is the process flow sheet of invention.
Figure: 1 -, 2 - spiral raw coal silo, weighing conveyor I, 3 - 1, 4 - lock valve, air dryer, drying, 5 - first stage separator,,,,,,, 6 hot blast stove of a cyclone separator,,,,,, 7, waste heat boiler,, 8 - hot blast stove two cyclone separator, the 9 -, 10 -, lock valve II, cooling blade machine,The 11 -, 12 -, mixer, heat rotary retort furnace, 13 - separator, 14 -, 15 - fluidized bed classification cooler, air lock valve III, 16 - grade cyclone separator,,, 17 - circulating fluidized bed hot blast stove,,,, 18 - screw metering conveyor II, 19 - lock valve IV,, the 20 -, 21 - combustion fan, hot blast furnace circulating fan, cooler, 22 circulating fan, 23 fan, discharge, 24 drying, two stage separator, 25 V, 26 lock valve, Venturi conveyer, conveying fan, 27 -, 28 -, cooling tower. Circulating pump, 29 -, 30 -, 31 - tar cooler, gas blower.
Embodiment
As shown in Figure 1, a kind of thermal barrier distillation system of coal, comprises run coal bin 1, pneumatic dryer 4, circulating fluid bed hot-air furnace 17.
Run coal bin 1 bottom is provided with spiral metering conveyor I 2, and this spiral metering conveyor I 2 is connected with pneumatic dryer 4 by blocking valve I 3; The top of pneumatic dryer 4 is connected with dry primary separator 5 by pipeline I, and one side is connected with hotblast stove secondary cyclone separator 8 by pipeline II; The top of dry primary separator 5 is connected with dry second-stage separator 24 by pipeline III, and its bottom is connected with mixing tank 11; The bottom of hotblast stove secondary cyclone separator 8 is provided with cooling blade machine 10, and one side is connected with waste heat boiler 7 by pipeline IV; The top of cooling blade machine 10 is provided with and cools back the mouth of a river, and its bottom is respectively equipped with cooling filling pipe end, blocking valve II 9, and this blocking valve II 9 is connected with ash content delivery pipe; The top of waste heat boiler 7 is provided with superheated vapour discharge outlet, and its bottom is provided with oiler feed mouth, and one side is connected with cyclonic separator 6 of hotblast stove; The bottom of a cyclonic separator 6 of hotblast stove is connected with mixing tank 11, and one side is connected with the top of circulating fluid bed hot-air furnace 17 by pipeline V; Mixing tank 11 bottoms are provided with interior hot rotary type gas retort 12, and one end of this interior hot rotary type gas retort 12 is connected with separator 13; The top of separator 13 is connected with cooling tower 28 by pipeline VI, and its bottom is connected with fluidized bed classification water cooler 14; The top of cooling tower 28 is provided with the coal gas discharge outlet being connected with gas fan 31, and its bottom is provided with tar emission mouth, and this tar emission mouth is connected with tar emission pipe, tar cooler 30 successively by recycle pump 29; Tar cooler 30 is connected with a side roof part of cooling tower 28; One side bottom of fluidized bed classification water cooler 14 is connected with semicoke output tube by blocking valve III 15, the bottom of its opposite side is connected with the top of dry second-stage separator 24 through pipeline VII by water cooler recirculation blower 22, and the top of its opposite side is connected with classification cyclonic separator 16; In pipeline VII, by discharge blower fan 23, be connected with chimney; The top of classification cyclonic separator 16 is connected with a side of circulating fluid bed hot-air furnace 17 respectively with bottom; The bottom of circulating fluid bed hot-air furnace 17 is connected with air input tube by burner blower 20, and its opposite side is provided with coal dust input aperture, raw coal input aperture, lime-ash discharge outlet, flue gas input aperture from top to bottom successively; Coal dust input aperture is connected with respectively blocking valve V 25, conveying fan 27 by Venturi handling machinery 26, and this blocking valve V 25 is connected with the bottom of dry second-stage separator 24; Raw coal input aperture is connected with spiral metering conveyor II 18 by input channel through blocking valve IV 19, and this spiral metering conveyor II 18 is connected with run coal bin 1; Flue gas input aperture is connected with pipeline VII by hotblast stove recirculation blower 21.
Wherein: interior hot rotary type gas retort 12 refers to lined revolving drum stove.
Mixing tank 11 is bin type mixing tank.
Cooling tower 28 refers to a kind of in packing tower, tray column or spray column.
Tar cooler 30 is shell and tube heat exchanger.
Pneumatic dryer 4 refers to a kind of in impulse pneumatic drying pipe, straight pipe type airflow drying tube, single hose airflow drying tube, Multi-tube airflow drying tube.
Dry primary separator 5 is decanter type separator or cyclonic separator.
Dry second-stage separator 24 refers to a kind of in cyclonic separator, sack cleaner or electric precipitator.
The application method of the thermal barrier distillation system of this coal, comprises the following steps:
(1) moisture is greater than after 15% be crushed to≤20mm of raw coal, send in run coal bin 1, and send in pneumatic dryer 4 by spiral metering conveyor I 2, blocking valve I 3, simultaneously, temperature after waste heat boiler 7 recovery part heats is that dedusting is separated again through hotblast stove secondary cyclone separator 8 for 300 ~ 800 ℃ of flue gases, this 300 ~ 800 flue gas enters that in pneumatic dryer 4, to carry out the dehydration of coal predrying, obtains respectively moisture content and be 1 ~ 8% coal dust and dried tail gas A after 2 ~ 5s.
(2) the coal dust that moisture content is 1 ~ 8% and dried tail gas A together send in dry primary separator 5 and carry out gas solid separation, obtain respectively coal dust and 90 ~ 150 ℃ of flue gases after separation; Coal dust after separation falls into mixing tank 11; 24 dedustings of 90 ~ 150 ℃ of flue gas drying second-stage separators, obtain respectively the coal dust of dried tail gas B and particle diameter < 0.5mm; Dried tail gas B discharges from dry second-stage separator 24 tops, and wherein a part drains into chimney by discharge blower fan 23, and rest part sends into respectively hotblast stove recirculation blower 21 and water cooler recirculation blower 22 recycles; The coal dust of particle diameter < 0.5mm is sent back in circulating fluid bed hot-air furnace 17 and is burned by Venturi handling machinery 26.
(3) the described raw coal in run coal bin 1 is sent into by circulating fluid bed hot-air furnace 17 bottoms through spiral metering conveyor II 18, blocking valve IV 19, simultaneously, air through burner blower 20 inputs is sent into by circulating fluid bed hot-air furnace 17 bottoms, the air of conveying fan 27 inputs is sent into by circulating fluid bed hot-air furnace 17 tops through Venturi handling machinery 26, and the part dried tail gas B that (2) step obtains is sent into by circulating fluid bed hot-air furnace 17 bottoms through hotblast stove recirculation blower 21, burns in the lump with separated solid phase; Obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash and lime-ash; Lime-ash is discharged through lime-ash discharge outlet.
(4) 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash are discharged and are entered cyclonic separator of hotblast stove 6 and carry out gas solid separation by circulating fluid bed hot-air furnace 17 tops, obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash.
(5) 800 ~ 1100 ℃ of circulating ash enter in mixing tank 11, (2) obtain with step separated after coal dust in the ratio of coal dust: circulating ash=1kg:1.8kg ~ 2.5kg, tentatively mix, obtain mixture; Mixture enters interior hot rotary type gas retort 12 by mixing tank 11, this interior hot rotary type gas retort 12 is done turning motion under motor drives, make mixture obtain sufficient mixed heat transfer, when being heated to 450 ~ 600 ℃, coal dust there is pyrogenation and carbonization reaction, after 5 ~ 60min, obtain respectively pyrolysis product, i.e. coal gas, tar and semicoke.
In pyrolysis product discharge, after hot rotary type gas retort 12, enter separator 13 and carry out gas solid separation, obtain respectively gaseous products and solid phase product; Gaseous products is sent into cooling tower 28 by separator 13 tops and is carried out oil gas refrigerated separation, obtains respectively coal gas and tar; Solid phase product is sent in fluidized bed classification water cooler 14 by separator 13 bottoms.
(6) the part dried tail gas B that (2) step obtains passes into from fluidized bed classification water cooler 14 bottoms by water cooler recirculation blower 22, (5) it is cooling that the solid phase product obtaining with step carries out fluidisation, obtains respectively semicoke product, the semicoke of granularity < 1mm and the mixture of circulating ash of granularity > 1mm; The semicoke product of granularity > 1mm is discharged by blocking valve III 15 continuously by fluidized bed classification water cooler 14 bottoms;
(7) the semicoke of granularity < 1mm and the mixture of circulating ash are discharged and to be entered classification cyclonic separator 16 and carry out gas solid separation by fluidized bed classification water cooler 14 tops under the effect of dried tail gas B, obtain respectively separated gas phase and separated solid phase; Separated gas phase is entered by the middle part of circulating fluid bed hot-air furnace 17; Separated solid is entered as circulating fuel by circulating fluid bed hot-air furnace 17 bottoms.
(8) 800 ~ 1100 ℃ of flue gases are sent into heating boiler water in waste heat boiler 7 and are reclaimed heat, and the flue gas after heat exchange, through the 8 further dedustings of hotblast stove secondary cyclone separator, obtains respectively ash content and dried tail gas C.
Ash content, is used as the building materials raw material of Building Materials Factory through blocking valve II 9 discharge systems by cooling blade machine 10.
Dried tail gas C sends into pneumatic dryer 4 and after 5 separation of super-dry primary separator, sends into further dedusting in dry second-stage separator 24, obtains respectively the coal dust of dried tail gas D and particle diameter < 0.5mm; Dried tail gas D discharges from dry second-stage separator 24 tops, and wherein a part drains into chimney by discharge blower fan 23, and rest part sends into respectively hotblast stove recirculation blower 21 and water cooler recirculation blower 22 recycles; The coal dust of particle diameter < 0.5mm is sent back in circulating fluid bed hot-air furnace 17 and is burned by Venturi handling machinery 26.
Claims (9)
1. the thermal barrier distillation system of a coal, comprise run coal bin (1), pneumatic dryer (4), circulating fluid bed hot-air furnace (17), it is characterized in that: described run coal bin (1) bottom is provided with spiral metering conveyor I (2), and this spiral metering conveyor I (2) is connected with described pneumatic dryer (4) by blocking valve I (3); The top of described pneumatic dryer (4) is connected with dry primary separator (5) by pipeline I, and one side is connected with hotblast stove secondary cyclone separator (8) by pipeline II; The top of described dry primary separator (5) is connected with dry second-stage separator (24) by pipeline III, and its bottom is connected with mixing tank (11); The bottom of described hotblast stove secondary cyclone separator (8) is provided with cooling blade machine (10), and one side is connected with waste heat boiler (7) by pipeline IV; The top of described cooling blade machine (10) is provided with and cools back the mouth of a river, and its bottom is respectively equipped with cooling filling pipe end, blocking valve II (9), and this blocking valve II (9) is connected with ash content delivery pipe; The top of described waste heat boiler (7) is provided with superheated vapour discharge outlet, and its bottom is provided with oiler feed mouth, and one side is connected with a cyclonic separator of hotblast stove (6); The bottom of a cyclonic separator of described hotblast stove (6) is connected with described mixing tank (11), and one side is connected with the top of described circulating fluid bed hot-air furnace (17) by pipeline V; Described mixing tank (11) bottom is provided with interior hot rotary type gas retort (12), and one end of this interior hot rotary type gas retort (12) is connected with separator (13); The top of described separator (13) is connected with cooling tower (28) by pipeline VI, and its bottom is connected with fluidized bed classification water cooler (14); The top of described cooling tower (28) is provided with the coal gas discharge outlet being connected with gas fan (31), and its bottom is provided with tar emission mouth, and this tar emission mouth is connected with tar emission pipe, tar cooler (30) successively by recycle pump (29); Described tar cooler (30) is connected with a side roof part of described cooling tower (28); One side bottom of described fluidized bed classification water cooler (14) is connected with semicoke output tube by blocking valve III (15), the bottom of its opposite side is connected with the top of described dry second-stage separator (24) through pipeline VII by water cooler recirculation blower (22), and the top of its opposite side is connected with classification cyclonic separator (16); In described pipeline VII, by discharge blower fan (23), be connected with chimney; The top of described classification cyclonic separator (16) is connected with a side of described circulating fluid bed hot-air furnace (17) respectively with bottom; The bottom of described circulating fluid bed hot-air furnace (17) is connected with air input tube by burner blower (20), and its opposite side is provided with coal dust input aperture, raw coal input aperture, lime-ash discharge outlet, flue gas input aperture from top to bottom successively; Described coal dust input aperture is connected with respectively blocking valve V (25), conveying fan (27) by Venturi handling machinery (26), and this blocking valve V (25) is connected with the bottom of described dry second-stage separator (24); Described raw coal input aperture is connected with spiral metering conveyor II (18) by input channel through blocking valve IV (19), and this spiral metering conveyor II (18) is connected with described run coal bin (1); Described flue gas input aperture is connected with described pipeline VII by hotblast stove recirculation blower (21).
2. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described interior hot rotary type gas retort (12) refers to lined revolving drum stove.
3. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described mixing tank (11) is bin type mixing tank.
4. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described cooling tower (28) refers to a kind of in packing tower, tray column or spray column.
5. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described tar cooler (30) is shell and tube heat exchanger.
6. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described pneumatic dryer (4) refers to a kind of in impulse pneumatic drying pipe, straight pipe type airflow drying tube, single hose airflow drying tube, Multi-tube airflow drying tube.
7. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described dry primary separator (5) is decanter type separator or cyclonic separator.
8. the thermal barrier distillation system of a kind of coal as claimed in claim 1, is characterized in that: described dry second-stage separator (24) refers to a kind of in cyclonic separator, sack cleaner or electric precipitator.
9. the application method of the thermal barrier distillation system of a kind of coal as claimed in claim 1, comprises the following steps:
(1) moisture is greater than after 15% be crushed to≤20mm of raw coal, send in run coal bin (1), and send in pneumatic dryer (4) by spiral metering conveyor I (2), blocking valve I (3), simultaneously, temperature after waste heat boiler (7) recovery part heat is that dedusting is separated again through hotblast stove secondary cyclone separator (8) for 300 ~ 800 ℃ of flue gases, this 300 ~ 800 flue gas enters that in described pneumatic dryer (4), to carry out the dehydration of coal predrying, obtains respectively moisture content and be 1 ~ 8% coal dust and dried tail gas A after 2 ~ 5s;
(2) the coal dust that described moisture content is 1 ~ 8% and described dried tail gas A together send in dry primary separator (5) and carry out gas solid separation, obtain respectively coal dust and 90 ~ 150 ℃ of flue gases after separation; Coal dust after described separation falls into mixing tank (11); Described 90 ~ 150 ℃ of flue gas drying second-stage separators (24) dedusting, obtains respectively the coal dust of dried tail gas B and particle diameter < 0.5mm; Described dried tail gas B discharges from described dry second-stage separator (24) top, and wherein a part drains into chimney by discharge blower fan (23), and rest part sends into respectively hotblast stove recirculation blower (21) and water cooler recirculation blower (22) recycles; The coal dust of described particle diameter < 0.5mm is sent back in circulating fluid bed hot-air furnace (17) and is burned by Venturi handling machinery (26);
By the described raw coal in described run coal bin (1) through spiral metering conveyor II (18), blocking valve IV (19) is sent into by circulating fluid bed hot-air furnace (17) bottom, simultaneously, air through burner blower (20) input is sent into by described circulating fluid bed hot-air furnace (17) bottom, the air of conveying fan (27) input is sent into by described circulating fluid bed hot-air furnace (17) top through Venturi handling machinery (26), and the described dried tail gas B of the part that (2) described step obtains is sent into by described circulating fluid bed hot-air furnace (17) bottom through hotblast stove recirculation blower (21), burn in the lump with described separated solid phase, obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash and lime-ash, described lime-ash is discharged through lime-ash discharge outlet,
(4) described 800 ~ 1100 ℃ of flue gases and described 800 ~ 1100 ℃ of circulating ash are discharged and to be entered a cyclonic separator of described hotblast stove (6) and carry out gas solid separation by described circulating fluid bed hot-air furnace (17) top, obtain respectively 800 ~ 1100 ℃ of flue gases and 800 ~ 1100 ℃ of circulating ash;
(5) described 800 ~ 1100 ℃ of circulating ash enter in described mixing tank (11), (2) obtain with described step separated after coal dust in the ratio of coal dust: circulating ash=1kg:1.8kg ~ 2.5kg, tentatively mix, obtain mixture; Described mixture enters interior hot rotary type gas retort (12) by described mixing tank (11), this interior hot rotary type gas retort (12) is done turning motion under motor drives, make mixture obtain sufficient mixed heat transfer, when being heated to 450 ~ 600 ℃, coal dust there is pyrogenation and carbonization reaction, after 5 ~ 60min, obtain respectively pyrolysis product, i.e. coal gas, tar and semicoke;
After the described pyrolysis product described interior hot rotary type gas retort of discharge (12), enter separator (13) and carry out gas solid separation, obtain respectively gaseous products and solid phase product; Described gaseous products is sent into cooling tower (28) by described separator (13) top and is carried out oil gas refrigerated separation, obtains respectively coal gas and tar; Described solid phase product is sent in fluidized bed classification water cooler (14) by described separator (13) bottom;
(6) the described dried tail gas B of part that (2) described step obtains passes into from described fluidized bed classification water cooler (14) bottom by water cooler recirculation blower (22), (5) it is cooling that the solid phase product obtaining with described step carries out fluidisation, obtains respectively semicoke product, the semicoke of granularity < 1mm and the mixture of circulating ash of granularity > 1mm; The semicoke product of described granularity > 1mm is discharged by blocking valve III (15) continuously by described fluidized bed classification water cooler (14) bottom;
(7) the semicoke of described granularity < 1mm and the mixture of circulating ash are discharged and to be entered classification cyclonic separator (16) and carry out gas solid separation by described fluidized bed classification water cooler (14) top under the effect of described dried tail gas B, obtain respectively separated gas phase and separated solid phase; The gas phase of described separation is entered by the middle part of circulating fluid bed hot-air furnace (17); The solid of described separation is entered as circulating fuel by described circulating fluid bed hot-air furnace (17) bottom;
(8) described 800 ~ 1100 ℃ of flue gases are sent into heating boiler water in described waste heat boiler (7) and are reclaimed heat, and the flue gas after heat exchange, through further dedusting of described hotblast stove secondary cyclone separator (8), obtains respectively ash content and dried tail gas C;
Described ash content, is used as the building materials raw material of Building Materials Factory through blocking valve II (9) discharge system by cooling blade machine (10);
Described dried tail gas C sends into described pneumatic dryer (4) and after described dry primary separator (5) separation, sends into further dedusting in dry second-stage separator (24), obtains respectively the coal dust of dried tail gas D and particle diameter < 0.5mm; Described dried tail gas D discharges from described dry second-stage separator (24) top, wherein a part drains into chimney by described discharge blower fan (23), and rest part sends into respectively described hotblast stove recirculation blower (21) and described water cooler recirculation blower (22) recycles; The coal dust of described particle diameter < 0.5mm is sent back in described circulating fluid bed hot-air furnace (17) and is burned by described Venturi handling machinery (26).
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| CN104017594B (en) * | 2014-06-20 | 2015-12-02 | 中煤能源黑龙江煤化工有限公司 | Coal low-temperature cracking process |
| CN104818035A (en) * | 2015-04-17 | 2015-08-05 | 龙口市中晟新能源科技开发有限公司 | Disk-type powdery substance pyrolysis device |
| CN105419879B (en) * | 2015-11-05 | 2020-07-10 | 东华工程科技股份有限公司 | Device and method for catalytic decomposition and high-temperature separation of coal substances |
| CN109489345B (en) * | 2018-12-26 | 2024-01-30 | 郑州博大浓缩干燥设备有限公司 | Air flow drying system for distillers' grains protein feed production |
| CN110862835B (en) * | 2019-12-03 | 2024-07-09 | 嘉禾聚能（天津）科技有限公司 | System for producing fuel gas |
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| CN101760222A (en) * | 2009-12-25 | 2010-06-30 | 山东天力干燥设备有限公司 | Novel fluidized bed semicoke production system and process thereof |
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