CN202968482U - Low-rank-coal pyrolysis and extraction equipment with down-circulating fluidized bed - Google Patents
Low-rank-coal pyrolysis and extraction equipment with down-circulating fluidized bed Download PDFInfo
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- CN202968482U CN202968482U CN 201220525585 CN201220525585U CN202968482U CN 202968482 U CN202968482 U CN 202968482U CN 201220525585 CN201220525585 CN 201220525585 CN 201220525585 U CN201220525585 U CN 201220525585U CN 202968482 U CN202968482 U CN 202968482U
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Abstract
The utility model provides a low-rank-coal pyrolysis and extraction equipment with a down-circulating fluidized bed. The low-rank-coal pyrolysis and extraction equipment comprises a low-rank-coal drying system, a semi-coke circulating system, a low-rank-coal reaction system and an extracted-coal forming system; the low-rank-coal drying system is communicated with the low-rank-coal reaction system through a rotating feeder; the low-rank-coal drying system is communicated with the semi-coke circulating system through a smoke fan; the semi-coke circulating system is communicated with the top of the low-rank-coal reaction system through a semi-coke heat carrier bin, and the semi-coke circulating system is communicated with the bottom of the low-rank-coal reaction system through a returning device; the low-rank-coal reaction system is communicated with the extracted-coal forming system through a hot semi-coke bin; the low-rank-coal drying system is communicated with the extracted-coal forming system through a hot coal bin; and the semi-coke circulating system is communicated with the extracted-coal forming system through a fine-coke bin.
Description
1. technical field
The utility model provides low-rank coal downlink cycle fluidized bed pyrolysis upgrading device, belongs to coal chemical technology.
2. background technology
China's low-rank coal reserves are abundant; has water-content high; oxygen level is high; the characteristics such as volatile matter is high, and calorific value is low produce more fine coal easy-weathering and spontaneous combustion under the condition of extensive mechanical mining of modern times; and the place of production is mostly in remote districts; have inconvenient traffic, make low-rank coal be not suitable for long-distance transport, application is very limited.China's low-rank coal is most of for direct combustion power generation at present, causes serious environmental pollution and a large amount of greenhouse gas emissions, and generating efficiency is low, and coal resources are made a low multiple use, serious waste of resources.It is that a kind of technological process is relatively simple and direct, investment is less, the technology of better economy that low-rank coal is carried out pyrolysis upgrading production high-quality semicoke while by-product coke oil and gas, not only solved energy long distance transportation, and can carry out comprehensive processing and utilization, has very strong competitive power, significant for China's development energy diversification strategy, meet national industrial policies and future thrust.It is also one of important development direction of the diversification energy.
The low-rank coal pyrolytic process can be divided into external-heat and internal heat type two classes by type of heating: external heating type heat efficient is low, the coal charge heating is uneven, the secondary of volatility product decomposes serious, tar yield is low, device is difficult to maximize, therefore this class technology is general only for the laboratory, and large industrialized pyrolysis of coal process is difficult to realize; Internal heat type technology utilization gaseous heat-carrier or solid thermal carriers are directly passed to coal charge to heat, make coal generation pyrolytic reaction, overcome the shortcoming of external-heat, have that the caloic transmission speed is fast, a homogeneous heating, fugitive constituent secondary decomposition of little, tar yield is high, and device is easy to the advantages such as maximization.
Internal heat type technique comprises gaseous heat-carrier pyrolytic process and solid heat carrier pyrolysis technique, wherein: the gaseous heat-carrier pyrolytic process is normally introduced the pyrolysis chamber with the flue gas of fuel combustion, two boiling bed process of representational COED technique, ENCOAL technique and Poland that the U.S. arranged etc.Solid heat carrier pyrolysis technique utilizes high temperature semicoke or other high-temp solid material to mix in the pyrolysis chamber with coal, utilizes the sensible heat of thermal barrier with pyrolysis of coal.Compare with the gaseous heat-carrier pyrolytic process, solid heat carrier pyrolysis has avoided volatility product that pyrolysis of coal separates out by flue gas dilution, has reduced simultaneously the load of cooling system, and process advantage is obvious.But there are the difficult problems such as band ash, mechanical moving element high temperature wear, device scale effect and equipment long-period stable operation in oil in existing low-rank coal solid heat carrier rapid pyrolysis technology, become the technical bottleneck of restriction low-rank coal fast pyrogenation, be badly in need of to eliminate according to low-rank coal pyrolytic reaction feature development that band ash, heat in oil are transmitted, the low order improving quality of coal by pyrolysis technology and equipment of reasonable energy utilization.
3. summary of the invention
The purpose of this utility model is exactly a kind of low-rank coal downlink cycle fluidized bed pyrolysis upgrading device that proposes for the deficiency that overcomes existing low order improving quality of coal by pyrolysis technology existence, both solved in the oil of low-rank coal fluidized bed pyrolysis upgrading and be with a grey difficult problem, heat energy and grizzle cohesiveness have rationally been utilized again, also obtain tar and the combustion gas of high added value, eliminated the upgraded coal Moisture Regain During.
The technical solution of the utility model:
The purpose of this utility model is by with low-rank coal and semicoke fractional separation, big-and-middle particulate coal and burnt by descending pyrolysis reactor pyrolysis, molecule coal and Jiao and part material coal and semicoke mixing upgrading, reach short mix, heat transfer, pyrolysis and separate, eliminate band ash oil from the source, utilize simultaneously grizzle cohesiveness to solve the difficult problem that upgraded coal is got damp.it is characterized in that low-rank coal downlink cycle fluidized bed pyrolysis upgrading device, by burning riser tube, gas distributor, inlet pipe, semicoke one-level gas-solid separator, the thermal barrier feed bin, semicoke secondary gas-solid separator, thin burnt feed bin, descending pyrolysis reactor, the oil gas gas-solid separator, oil gas vent, material distributing valve, hot semicoke feed bin, low-rank coal upgrading down mixing pipe, induced draft fan, the flue gas riser tube, flue gas one-level gas-solid separator, the top feed bin, rotory feeder, flue gas secondary gas-solid separator, exhanst gas outlet, the low-rank coal entrance, lift, modified coal bunker, thermoforming machine, the outlet of upgrading moulded coal, the hot coal feed bin, the returning charge valve forms.Low-rank coal downlink cycle fluidized bed pyrolysis upgrading device is divided into low-rank coal dehumidification system, the semicoke recycle system, low-rank coal reactive system, upgraded coal formation system four parts, the low-rank coal dehumidification system is communicated with by rotory feeder with the low-rank coal reactive system, the low-rank coal dehumidification system is communicated with by smoke induced draught fan with the semicoke recycle system, the semicoke recycle system and low-rank coal reactive system top by semicoke thermal barrier feed bin be communicated with, the bottom is communicated with by material returning device; Low-rank coal reactive system and upgraded coal formation system are communicated with by hot semicoke feed bin, and low-rank coal dehumidification system and upgraded coal formation system are communicated with by the hot coal feed bin, and the semicoke recycle system and upgraded coal formation system are communicated with by thin burnt feed bin.
The low-rank coal coal drying system is flue gas riser tube bottom low-rank coal entrance, and the top is provided with flue gas one-level gas-solid separator and flue gas secondary gas-solid separator; Flue gas one-level gas-solid separator solid outlet access top feed bin, then be connected to descending pyrolysis reactor top through rotory feeder, pneumatic outlet is connected with the entrance of flue gas secondary gas-solid separator; Flue gas secondary gas-solid separator solid outlet access hot coal feed bin, by material valve connection low-rank coal upgrading down mixing pipe top, pneumatic outlet is as exhanst gas outlet.
The low-rank coal reactive system be descending pyrolysis reactor top by rotory feeder be connected the top feed bin and connect, be connected with the thermal barrier feed bin by the material valve, the oil gas gas-solid separator is accessed in the bottom; The oil gas vent of oil gas gas-solid separator connects the separation system in downstream, and solid outlet is divided into two by material distributing valve, and the returning charge valve of leading up to enters and burns riser tube bottom, and the one tunnel hot semicoke feed bin of access is communicated with low-rank coal upgrading down mixing pipe top by the material valve.
The upgraded coal formation system is that low-rank coal upgrading down mixing pipe top is connected with the low-rank coal dehumidification system by the hot coal feed bin, be connected with the low-rank coal reactive system by hot semicoke feed bin, be connected with the semicoke recycle system by thin burnt feed bin, be connected with lift by modified coal bunker simultaneously; Low-rank coal upgrading down mixing pipe bottom is connected with the thermoforming machine entrance, exports to be the outlet of upgrading moulded coal.
The semicoke recycle system is provided with inlet pipe and gas distributor for burning riser tube bottom, is communicated with the low-rank coal reactive system by the returning charge valve; The top is provided with semicoke one-level gas-solid separator and semicoke secondary gas-solid separator, semicoke one-level gas-solid separator solid outlet access thermal barrier feed bin, and by the material valve descending pyrolysis reactor of access top, pneumatic outlet is connected with semicoke secondary gas-solid separator entrance; The thin burnt feed bin of semicoke secondary gas-solid separator solid outlet access, by material valve access low-rank coal upgrading down mixing pipe top, pneumatic outlet is communicated with bottom the flue gas riser tube by induced draft fan.
Burning riser tube is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2～2: 1.
Burn riser tube bottom upwards 200mm-1500mm be the returning charge mouth of returning charge valve, a kind of for in the on-mechanical valve such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and the mechanical valve such as hydraulic pressure slip plug valve, electronic slip plug valve of returning charge valve, optimal selection is U-shaped material returning device.
The flue gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and optimal selection is horizontal cyclone separator.
The semicoke gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and the optimal selection of semicoke one-level gas-solid separator is inertial separator, and the optimal selection of semicoke secondary gas-solid separator is vertical cyclone separator.
Descending pyrolysis reactor aspect ratio is 15-100, and top is provided with the static mixer of grating, and the height of static mixer is 300mm-5000mm.
The oil gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and optimal selection is vertical cyclone separator.
Down mixing pipe aspect ratio is 10-30, and top is provided with the static mixer of grating, and the height of static mixer is 100mm-3000mm.
Thermoforming machine is two roller forming machines, screw extruding briquetting machine, rotating disc type single-lead-screw extruding briquetting machine or ring type single-lead-screw extruding briquetting machine, and optimal selection is two roller forming machines.
The utility model is described in detail characteristics of the present invention with embodiment.
4. description of drawings
Accompanying drawing is structural representation of the present utility model.
The drawing of accompanying drawing is established bright as follows:
1, burn riser tube 2, gas distributor 3, inlet pipe 4, semicoke one-level gas-solid separator 5, thermal barrier feed bin 6, semicoke secondary gas-solid separator 7, thin burnt feed bin 8, descending pyrolysis reactor 9, oil gas gas-solid separator 10, oil gas vent 11, material distributing valve 12, hot semicoke feed bin 13, low-rank coal upgrading down mixing pipe 14, induced draft fan 15, flue gas riser tube 16, flue gas one-level gas-solid separator 17, top feed bin 18, rotory feeder 19, flue gas secondary gas-solid separator 20, exhanst gas outlet 21, low-rank coal entrance 22, lift 23, modified coal bunker 24, thermoforming machine 25, upgrading moulded coal outlet 26, the hot coal feed bin.
Below in conjunction with drawings and Examples in detail constructional feature of the present utility model is described in detail.
5. embodiment
low-rank coal downlink cycle fluidized bed pyrolysis upgrading device, by burning riser tube (1), gas distributor (2), inlet pipe (3), semicoke one-level gas-solid separator (4), thermal barrier feed bin (5), semicoke secondary gas-solid separator (6), thin burnt feed bin (7), descending pyrolysis reactor (8), oil gas gas-solid separator (9), oil gas vent (10), material distributing valve (11), hot semicoke feed bin (12), low-rank coal upgrading down mixing pipe (13), induced draft fan (14), flue gas riser tube (15), flue gas one-level gas-solid separator (16), top feed bin (17), rotory feeder (18), flue gas secondary gas-solid separator (19), exhanst gas outlet (20), low-rank coal entrance (21), lift (22), modified coal bunker (23), thermoforming machine (24), upgrading moulded coal outlet (25), hot coal feed bin (26), returning charge valve (27) forms.Low-rank coal downlink cycle fluidized bed pyrolysis upgrading device is divided into low-rank coal dehumidification system, the semicoke recycle system, low-rank coal reactive system, upgraded coal formation system four parts, the low-rank coal dehumidification system is communicated with by rotory feeder with the low-rank coal reactive system, the low-rank coal dehumidification system is communicated with by smoke induced draught fan with the semicoke recycle system, the semicoke recycle system and low-rank coal reactive system top by semicoke thermal barrier feed bin be communicated with, the bottom is communicated with by material returning device; Low-rank coal reactive system and upgraded coal formation system are communicated with by hot semicoke feed bin, and low-rank coal dehumidification system and upgraded coal formation system are communicated with by the hot coal feed bin, and the semicoke recycle system and upgraded coal formation system are communicated with by thin burnt feed bin.
The low-rank coal coal drying system is flue gas riser tube (15) bottom low-rank coal entrance (21), and the top is provided with flue gas one-level gas-solid separator (16) and flue gas secondary gas-solid separator (19); Flue gas one-level gas-solid separator (16) solid outlet access top feed bin (17), be connected to descending pyrolysis reactor (8) top through rotory feeder (18) again, pneumatic outlet is connected with the entrance of flue gas secondary gas-solid separator (19); Flue gas secondary gas-solid separator (19) solid outlet access hot coal feed bin (26), by material valve connection low-rank coal upgrading down mixing pipe (13) top, pneumatic outlet is as exhanst gas outlet (20).
The low-rank coal reactive system be descending pyrolysis reactor (8) top by rotory feeder (18) with is connected top feed bin (17) and connects, by expecting that valve is connected with thermal barrier feed bin (26), oil gas gas-solid separator (9) is accessed in the bottom; Oil gas gas-solid separator (9) oil gas vent connects the separation system in downstream, solid outlet is divided into two by material distributing valve (11), the returning charge valve of leading up to enters and burns riser tube (1) bottom, and the one tunnel hot semicoke feed bin of access (12) is communicated with low-rank coal upgrading down mixing pipe (13) top by the material valve.
The upgraded coal formation system is that low-rank coal upgrading down mixing pipe (13) top is connected with the low-rank coal dehumidification system by hot coal feed bin (26), be connected with the low-rank coal reactive system by hot semicoke feed bin (12), be connected with the semicoke recycle system by thin burnt feed bin (7), be connected with lift (22) by modified coal bunker (23) simultaneously; Low-rank coal upgrading down mixing pipe (13) bottom is connected with thermoforming machine (24) entrance, exports to be upgrading moulded coal outlet (25).
The semicoke recycle system is provided with inlet pipe (3) and gas distributor (2) for burning riser tube (1) bottom, is communicated with the low-rank coal reactive system by returning charge valve (27); The top is provided with semicoke one-level gas-solid separator (4) and semicoke secondary gas-solid separator (6), semicoke one-level gas-solid separator (4) solid outlet access thermal barrier feed bin (26), by material valve access descending pyrolysis reactor (8) top, pneumatic outlet is connected with semicoke secondary gas-solid separator (6) entrance; Semicoke secondary gas-solid separator (6) solid outlet access thin burnt feed bin (7), by material valve access low-rank coal upgrading down mixing pipe (13) top, pneumatic outlet is communicated with bottom flue gas riser tube (15) by induced draft fan (14).
Burning riser tube (1) is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2～2: 1.
Burn riser tube (1) bottom upwards 200mm-1500mm be the returning charge mouth of returning charge valve (27), returning charge valve (27) is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and the mechanical valve such as hydraulic pressure slip plug valve, electronic slip plug valve, and optimal selection is U-shaped material returning device.
The flue gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and optimal selection is horizontal cyclone separator.
The semicoke gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and the optimal selection of semicoke one-level gas-solid separator is inertial separator, and the optimal selection of semicoke secondary gas-solid separator is vertical cyclone separator.
Descending pyrolysis reactor (8) aspect ratio is 15-100, and top is provided with the static mixer of grating, and the height of static mixer is 300mm-5000mm.
The oil gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and optimal selection is vertical cyclone separator.
Down mixing pipe (13) aspect ratio is 10-30, and top is provided with the static mixer of grating, and the height of static mixer is 100mm-3000mm.
Thermoforming machine (24) is two roller forming machines, screw extruding briquetting machine, rotating disc type single-lead-screw extruding briquetting machine or ring type single-lead-screw extruding briquetting machine, and optimal selection is two roller forming machines.
During concrete operation, a large amount of low-rank coal less than 6mm are entered flue gas riser tube (15) drying and promote through low-rank coal entrance (21), the low-rank coal particle is by flue gas one-level gas-solid separator (16) and flue gas secondary gas-solid separator (19) fractional separation, flue gas effluxes from exhanst gas outlet (20), big-and-middle particle enters top feed bin (17), and fine particle enters hot coal feed bin (26) and flows into low-rank coal upgrading down mixing pipe (13) by the material valve; Big-and-middle particle low-rank coal through rotory feeder (18) on descending pyrolysis reactor (8) top with the high temperature circulation semicoke that falls by the material valve realize rapidly from mix, intensification, pyrolysis, at descending pyrolysis reactor (8) standpipe bottom oil gas and semicoke sharp separation under oil gas gas-solid separator (9) acts on; Pyrolysis oil gas is discharged through condenser from oil gas vent (10) and is obtained liquid product and coal gas, and semicoke is divided into two through material distributing valve (11); The part semicoke enters hot semicoke feed bin (12) and flows into low-rank coal upgrading down mixing pipe (13) by the material valve, and the part semicoke enters by the returning charge valve and burns air mixed, the combustion heating that riser tube (1) and inlet pipe (3) and gas distributor (2) come; high temperature semicoke after heating through semicoke one-level gas-solid separator (4) and semicoke secondary gas-solid separator (6) with after flue gas separates, flue gas guided to by induced draft fan (14) that flue gas riser tube (15) bottom promotes and dry from low-rank coal entrance (21) add less than the 6mm low-rank coal, big-and-middle particle enters thermal barrier feed bin (5) and flows into descending pyrolysis reactor (8) top as the high temperature circulation semicoke, realize the semicoke circulation heating, thin semicoke enters thin burnt feed bin (7) and flows into low-rank coal upgrading down mixing pipe (13) by the material valve, mention modified coal bunker (23) less than the low-rank coal of 6mm by lift (22) on a small quantity, through the material valve the semicoke of low-rank coal upgrading down mixing pipe (13) top and inflow and hot coal realize rapidly from mix, heat exchange, part soften pyrolysis, mixing coal tar after cooling flows into thermoforming machine (24) and produces the upgrading moulded coal from upgrading moulded coal outlet (25) discharge.
Burning riser tube (1) temperature of reaction is 850 ℃-1200 ℃.
The blending ratio of high temperature semicoke and big-and-middle particle low-rank coal is 3-8: 1.
Descending pyrolysis reactor (8) outlet temperature of reaction is 450 ℃-600 ℃.
Low-rank coal upgrading down mixing pipe (13) outlet temperature of reaction is 100 ℃-300 ℃.
Fine coal combined cyclic fluidized bed classification pyrolytic gasification equipment provided by the utility model, by with low-rank coal and semicoke fractional separation, big-and-middle particulate coal and burnt by descending pyrolysis reactor pyrolysis, molecule coal and Jiao and part material coal and semicoke mixing upgrading, reach short mix, heat transfer, pyrolysis and separate, eliminate band ash oil from the source, the tar yield is the 95%-120% of theoretical oil yield, well cuts content is less than 0.5%, Btu utilization is reasonable, utilizes simultaneously grizzle cohesiveness to solve the difficult problem that upgraded coal is got damp.
Claims (10)
1. low-rank coal downlink cycle fluidized bed pyrolysis upgrading device is by burning riser tube, gas distributor, inlet pipe, semicoke one-level gas-solid separator, the thermal barrier feed bin, semicoke secondary gas-solid separator, thin burnt feed bin, descending pyrolysis reactor, the oil gas gas-solid separator, oil gas vent, material distributing valve, hot semicoke feed bin, low-rank coal upgrading down mixing pipe, induced draft fan, the flue gas riser tube, flue gas one-level gas-solid separator, the top feed bin, rotory feeder, flue gas secondary gas-solid separator, exhanst gas outlet, the low-rank coal entrance, lift, modified coal bunker, thermoforming machine, the outlet of upgrading moulded coal, the hot coal feed bin, the returning charge valve forms, and it is characterized in that low-rank coal downlink cycle fluidized bed pyrolysis upgrading device is divided into the low-rank coal dehumidification system, the semicoke recycle system, the low-rank coal reactive system, upgraded coal formation system four parts, the low-rank coal dehumidification system is communicated with by rotory feeder with the low-rank coal reactive system, the low-rank coal dehumidification system is communicated with by smoke induced draught fan with the semicoke recycle system, and the semicoke recycle system and low-rank coal reactive system top are communicated with by semicoke thermal barrier feed bin, the bottom is communicated with by material returning device, low-rank coal reactive system and upgraded coal formation system are communicated with by hot semicoke feed bin, and low-rank coal dehumidification system and upgraded coal formation system are communicated with by the hot coal feed bin, and the semicoke recycle system and upgraded coal formation system are communicated with by thin burnt feed bin.
2. carry according to claim 1 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that the low-rank coal dehumidification system is flue gas riser tube bottom low-rank coal entrance, the top is provided with flue gas one-level gas-solid separator and flue gas secondary gas-solid separator; Flue gas one-level gas-solid separator solid outlet access top feed bin, then be connected to descending pyrolysis reactor top through rotory feeder, pneumatic outlet is connected with the entrance of flue gas secondary gas-solid separator; Flue gas secondary gas-solid separator solid outlet access hot coal feed bin, by material valve connection low-rank coal upgrading down mixing pipe top, pneumatic outlet is as exhanst gas outlet.
3. carry according to claim 1 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that the low-rank coal reactive system be descending pyrolysis reactor top by rotory feeder be connected the top feed bin and connect, be connected bottom access oil gas gas-solid separator with the thermal barrier feed bin by the material valve; The oil gas vent of oil gas gas-solid separator connects the separation system in downstream, and solid outlet is divided into two by material distributing valve, and the returning charge valve of leading up to enters and burns riser tube bottom, and the one tunnel hot semicoke feed bin of access is by material valve and low-rank coal upgrading down mixing pipe top UNICOM.
4. carry according to claim 1 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that the upgraded coal formation system is that low-rank coal upgrading down mixing pipe top is connected with the low-rank coal dehumidification system by the hot coal feed bin, be connected with the low-rank coal reactive system by hot semicoke feed bin, be connected with the semicoke recycle system by thin burnt feed bin, be connected with lift by modified coal bunker simultaneously; Low-rank coal upgrading down mixing pipe bottom is connected with the thermoforming machine entrance, exports to be the outlet of upgrading moulded coal.
5. carry according to claim 1 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that the semicoke recycle system is provided with inlet pipe and gas distributor for burning riser tube bottom, is communicated with the low-rank coal reactive system by the returning charge valve; The top is provided with semicoke one-level gas-solid separator and semicoke secondary gas-solid separator, semicoke one-level gas-solid separator solid outlet access thermal barrier feed bin, and by the material valve descending pyrolysis reactor of access top, pneumatic outlet is connected with semicoke secondary gas-solid separator entrance; The thin burnt feed bin of semicoke secondary gas-solid separator solid outlet access, by material valve access low-rank coal upgrading down mixing pipe top, pneumatic outlet is communicated with bottom the flue gas riser tube by induced draft fan.
6. carry according to claim 5 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that burning riser tube is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2～2: 1.
7. carry according to claim 5 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that burning riser tube bottom upwards 200mm-1500mm be the returning charge mouth of returning charge valve, the returning charge valve is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and the mechanical valve such as hydraulic pressure slip plug valve, electronic slip plug valve, and optimal selection is U-shaped material returning device; The semicoke gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and the optimal selection of semicoke one-level gas-solid separator is inertial separator, and the optimal selection of semicoke secondary gas-solid separator is vertical cyclone separator.
8. carry according to claim 4 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that down mixing pipe aspect ratio is 10-30, top is provided with the static mixer of grating, and the height of static mixer is 100mm-3000mm; Thermoforming machine is two roller forming machines, screw extruding briquetting machine, rotating disc type single-lead-screw extruding briquetting machine or ring type single-lead-screw extruding briquetting machine, and optimal selection is two roller forming machines.
9. carry according to claim 3 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that descending pyrolysis reactor aspect ratio is 15-100, top is provided with the static mixer of grating, and the height of static mixer is 300mm-5000mm; The oil gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, and optimal selection is vertical cyclone separator.
10. carry according to claim 2 the low-rank coal downlink cycle fluidized bed pyrolysis upgrading device of stating, it is characterized in that the flue gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator, optimal selection is horizontal cyclone separator.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220525585 CN202968482U (en) | 2012-10-11 | 2012-10-11 | Low-rank-coal pyrolysis and extraction equipment with down-circulating fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220525585 CN202968482U (en) | 2012-10-11 | 2012-10-11 | Low-rank-coal pyrolysis and extraction equipment with down-circulating fluidized bed |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102994126A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis upgrading equipment of downward circulating fluidized bed for low-rank coal |
| CN104444372A (en) * | 2013-09-24 | 2015-03-25 | 中国石油大学(华东) | Powder low-energy-consumption high-pressure conveying process |
-
2012
- 2012-10-11 CN CN 201220525585 patent/CN202968482U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102994126A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis upgrading equipment of downward circulating fluidized bed for low-rank coal |
| CN102994126B (en) * | 2012-10-11 | 2014-07-16 | 田原宇 | Pyrolysis upgrading equipment of downward circulating fluidized bed for low-rank coal |
| CN104444372A (en) * | 2013-09-24 | 2015-03-25 | 中国石油大学(华东) | Powder low-energy-consumption high-pressure conveying process |
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