CN202912905U - Pyrolysis liquefaction equipment of oil shale downward circulating fluid bed - Google Patents
Pyrolysis liquefaction equipment of oil shale downward circulating fluid bed Download PDFInfo
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- CN202912905U CN202912905U CN 201220525249 CN201220525249U CN202912905U CN 202912905 U CN202912905 U CN 202912905U CN 201220525249 CN201220525249 CN 201220525249 CN 201220525249 U CN201220525249 U CN 201220525249U CN 202912905 U CN202912905 U CN 202912905U
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Abstract
The utility model provides pyrolysis liquefaction equipment of an oil shale downward circulating fluid bed. A gas inlet pipe, a gas distributor, an auxiliary fuel inlet and a material return valve are arranged at the bottom of a coke-burning lifting pipe; a hot ash gas-solid separator is arranged at the top of the coke-burning lifting pipe; a solid outlet of a hot ash primary gas-solid separator is connected to a heat carrier bin and connected to the top of a downward pyrolysis reactor through a material valve; a gas outlet of the hot ash primary gas-solid separator is connected with an inlet of a hot ash secondary gas-solid separator; a solid outlet of the hot ash secondary gas-solid separator is connected to cooling bin for discharging; a gas outlet of the hot ash secondary gas-solid separator is communicated with the bottom of a flue gas lifting pipe through an induced draft fan; an oil shale powder is formed at the bottom of the flue gas lifting pipe; a flue gas gas-solid separator is arranged at the top of the flue gas lifting pipe; a solid outlet of the flue gas gas-solid separator is connected to an upper bin and is connected with the top end of the downward pyrolysis reactor through a rotary feeder; an gas outlet of the flue gas gas-solid separator is served as a flue gas outlet; the bottom of the downward pyrolysis reactor is connected to an oil gas gas-solid separator; an oil gas outlet of the oil gas gas-solid separator is connected with a downstream separating system; and a solid outlet of the oil gas gas-solid separator enters the bottom of the coke-burning lifting pipe through the material return valve.
Description
1. technical field
The utility model provides resinous shale downlink cycle fluidized bed pyrolysis liquefaction device, belongs to the refining of petroleum field.
2. background technology
Resinous shale belongs to unconventional petroleum resources, is listed in the very important energy of taking over of 21 century with the feasibility of aboundresources and development and use.China's oil shale resources are abundant, about 2,400 hundred million tons of technology mining resources amount, and recyclable empyreumatic oil is about 10,000,000,000 tons in theory, and industrialization potential is huge.
At present, many countries all are studied dry distillation method of oil shale in the world, the formation suitability for industrialized production scale that has.Oil shale distillation 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 resinous shale 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 oil shale pyrolysis process is difficult to realize; Internal heat type technology utilization gaseous heat-carrier or solid thermal carriers are directly passed to resinous shale to heat, make resinous shale 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 then utilizes high temperature semicoke or other high-temp solid material to mix in the pyrolysis chamber with resinous shale, utilizes the sensible heat of thermal barrier with oil shale pyrolysis.Compare with the gaseous heat-carrier pyrolytic process, solid heat carrier pyrolysis has avoided volatility product that oil shale pyrolysis 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 the oil in existing resinous shale solid heat carrier rapid pyrolysis technology, become the technical bottleneck of restriction resinous shale fast pyrogenation, be badly in need of to eliminate according to the exploitation of oil shale pyrolysis response characteristic that band ash, heat in the oil are transmitted, oil shale pyrolysis liquefaction technology and the equipment of reasonable energy utilization.
3. summary of the invention
The purpose of this utility model is exactly a kind of resinous shale downlink cycle fluidized bed pyrolysis liquefaction device that proposes for the deficiency that overcomes existing oil shale pyrolysis liquefaction technology existence, both solved in the oil of oil shale fluidized bed pyrolysis upgrading and be with a grey difficult problem, rationally utilize again heat energy, also obtained tar and the combustion gas of high added value.
The technical solution of the utility model:
Resinous shale downlink cycle fluidized bed pyrolysis liquefaction device, by burning riser tube, gas distributor, inlet pipe, the grey one-level gas-solid separator of heat, the thermal barrier feed bin, the grey secondary gas-solid separator of heat, the cooling feed bin, descending pyrolysis reactor, the oil gas gas-solid separator, oil gas vent, material returning device, auxiliary coal fuel inlet, resinous shale powder entrance, induced draft fan, the flue gas riser tube, the oil shale gas solid separator, the top feed bin, rotory feeder, exhanst gas outlet forms, it is characterized in that burning the riser tube bottom and be provided with inlet pipe and gas distributor, bottom sides is provided with auxiliary fuel entrance and returning charge valve, the top is provided with hot grey one-level gas-solid separator and hot grey secondary gas-solid separator, the grey one-level gas-solid separator solid outlet access of heat thermal barrier feed bin, access descending pyrolysis reactor top by the material valve, pneumatic outlet links to each other with the grey secondary gas-solid separator of heat entrance; The grey secondary gas-solid separator solid outlet access of heat cooling feed bin effluxes, and pneumatic outlet is communicated with flue gas riser tube bottom by induced draft fan; Flue gas riser tube bottom is provided with resinous shale powder entrance, and the top is provided with the oil shale gas solid separator; Oil shale gas solid separator solid outlet access top feed bin is connected to descending pyrolysis reactor top through rotory feeder again, and pneumatic outlet is as exhanst gas outlet; Descending pyrolysis reactor bottom access oil gas gas-solid separator; The oil gas vent of oil gas gas-solid separator connects the separation system in downstream, and solid outlet enters by the returning charge valve and burns the riser tube bottom.
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 and be by diameter is that the big or small straight tube of riser tube gasifying reactor equivalent diameter different multiples is formed by connecting by the concentric reducer pipe fitting, and the diameter ratio of big or small straight tube is 1.2～2: 1.
Burn riser tube bottom upwards 200mm-1500mm be returning charge mouth and the auxiliary coal fuel inlet 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 grey gas-solid separator of heat is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, and the optimal selection of hot grey one-level gas-solid separator is inertial separator, and the optimal selection of hot grey 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, the inertial separator, and optimal selection is vertical cyclone separator.
The oil shale gas solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, and optimal selection is inertial separator.
The utility model is described in detail characteristics of the present utility model 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, burns riser tube 2, gas distributor 3, inlet pipe 4, hot grey one-level gas-solid separator 5, thermal barrier feed bin 6, hot grey secondary gas-solid separator 7, cooling feed bin 8, descending pyrolysis reactor 9, oil gas gas-solid separator 10, oil gas vent 11, material returning device 12, auxiliary coal fuel inlet 13, resinous shale powder entrance 14, induced draft fan 15, flue gas riser tube 16, oil shale gas solid separator 17, top feed bin 18, rotory feeder 19, exhanst gas outlet.
Below in conjunction with drawings and Examples in detail process characteristic of the present utility model is described in detail.
5. embodiment
Resinous shale downlink cycle fluidized bed pyrolysis liquefaction device, by burning riser tube (1), gas distributor (2), inlet pipe (3), heat grey one-level gas-solid separator (4), thermal barrier feed bin (5), heat grey secondary gas-solid separator (6), cooling feed bin (7), descending pyrolysis reactor (8), oil gas gas-solid separator (9), oil gas vent (10), material returning device (11), auxiliary coal fuel inlet (12), resinous shale powder entrance (13), induced draft fan (14), flue gas riser tube (15), oil shale gas solid separator (16), top feed bin (17), rotory feeder (18), exhanst gas outlet (19) forms, it is characterized in that burning riser tube (1) bottom and be provided with inlet pipe (3) and gas distributor (2), bottom sides is provided with auxiliary fuel entrance (12) and returning charge valve (11), the top is provided with hot grey one-level gas-solid separator (4) and hot grey secondary gas-solid separator (6), heat grey one-level gas-solid separator (4) solid outlet access thermal barrier feed bin (5), access descending pyrolysis reactor (8) top by the material valve, pneumatic outlet links to each other with hot grey secondary gas-solid separator (6) entrance; Heat grey secondary gas-solid separator (6) solid outlet access cooling feed bin (7) effluxes, and pneumatic outlet is communicated with flue gas riser tube (15) bottom by induced draft fan (14); Flue gas riser tube (15) bottom is provided with resinous shale powder entrance (13), and the top is provided with oil shale gas solid separator (16); Oil shale gas solid separator (16) solid outlet access top feed bin (17) is connected to descending pyrolysis reactor (8) top through rotory feeder (18) again, and pneumatic outlet is as exhanst gas outlet (19); Descending pyrolysis reactor (8) bottom access oil gas gas-solid separator (9); The oil gas vent of oil gas gas-solid separator (9) connects the separation system in downstream, and solid outlet enters by returning charge valve (11) and burns riser tube bottom (1).
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 and be by diameter is that the big or small straight tube of riser tube gasifying reactor equivalent diameter different multiples is formed by connecting by the concentric reducer pipe fitting, and the diameter ratio of big or small straight tube is 1.2～2: 1.
Burn riser tube (1) bottom upwards 200mm-1500mm be returning charge mouth and the auxiliary coal fuel inlet (12) of returning charge valve (11), 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 (11), optimal selection is U-shaped material returning device.
The grey gas-solid separator of heat is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, and the optimal selection of hot grey one-level gas-solid separator is inertial separator, and the optimal selection of hot grey 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.
Oil gas gas-solid separator (9) is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, and optimal selection is vertical cyclone separator.
Oil shale gas solid separator (16) is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, and optimal selection is inertial separator.
During concrete operations, a large amount of resinous shale less than 6mm are entered (the 150 dry and liftings of flue gas riser tube through resinous shale powder entrance (13), oil shale particle is separated by oil shale gas solid separator (16), flue gas effluxes from exhanst gas outlet (19), oil shale particle enters top feed bin (17) and realizes rapidly from mixing with the high temperature circulation heat ash that falls by the material valve on descending pyrolysis reactor (8) top through rotory feeder (18), heat up, pyrolysis is at descending reactor (8) standpipe bottom oil gas, heat ash and semicoke sharp separation under oil gas gas-solid separator (9) effect; Pyrolysis oil gas is discharged through condenser from oil gas vent (10) and is obtained liquid product and dry gas, and the returning charge valve (11) that heat ash and semicoke are carried by air enters together air mixed, the combustion heating next with inlet pipe (3) and gas distributor (2) of the coal that burns riser tube (1) and come from auxiliary coal fuel inlet (12); High warm ash after the heating through the grey one-level gas-solid separator of heat (4) and hot grey secondary gas-solid separator (6) with after flue gas separates, flue gas is guided to by induced draft fan (14) that flue gas riser tube (15) bottom promotes and is dry from from the resinous shale powder of resinous shale powder entrance (13) less than 6mm, the hot ash of big-and-middle particle enters thermal barrier feed bin (5) and flows into descending pyrolysis reactor (8) top as high temperature circulation heat ash, realize hot grey circulation heating, after entering cooling feed bin (7), thin ash effluxes comprehensive utilization, both from having solved the oil of fluidized bed pyrolysis pyrolysis, the source was with a grey difficult problem, rationally utilize again heat energy, also obtained tar and the dry gas of high added value.
Burning riser tube (1) temperature of reaction is 850 ℃-1200 ℃.
The blending ratio of high warm ash and resinous shale powder is 4-10: 1.
Descending pyrolysis reactor (8) outlet temperature of reaction is 450 ℃-600 ℃.
Resinous shale downlink cycle fluidized bed pyrolysis liquefaction device provided by the utility model, by with the grey fractional separation of heat, big-and-middle particle heat ash effluxes by descending pyrolysis reactor pyrolysis, the hot ash of molecule, reach short mix, heat transfer, pyrolysis and separate, eliminate band ash the oil from the source, the tar yield is the 95%-120% of theoretical oil yield, and well cuts content is less than 0.5%, and Btu utilization is reasonable.
Claims (7)
1. resinous shale downlink cycle fluidized bed pyrolysis liquefaction device, by burning riser tube, gas distributor, inlet pipe, the grey one-level gas-solid separator of heat, the thermal barrier feed bin, the grey secondary gas-solid separator of heat, the cooling feed bin, descending pyrolysis reactor, the oil gas gas-solid separator, oil gas vent, material returning device, auxiliary coal fuel inlet, resinous shale powder entrance, induced draft fan, the flue gas riser tube, the oil shale gas solid separator, the top feed bin, rotory feeder, exhanst gas outlet forms, it is characterized in that burning the riser tube bottom and be provided with inlet pipe and gas distributor, bottom sides is provided with auxiliary fuel entrance and returning charge valve, the top is provided with hot grey one-level gas-solid separator and hot grey secondary gas-solid separator, the grey one-level gas-solid separator solid outlet access of heat thermal barrier feed bin, access descending pyrolysis reactor top by the material valve, pneumatic outlet links to each other with the grey secondary gas-solid separator of heat entrance; The grey secondary gas-solid separator solid outlet access of heat cooling feed bin effluxes, and pneumatic outlet is communicated with flue gas riser tube bottom by induced draft fan; Flue gas riser tube bottom is provided with resinous shale powder entrance, and the top is provided with the oil shale gas solid separator; Oil shale gas solid separator solid outlet access top feed bin is connected to descending pyrolysis reactor top through rotory feeder again, and pneumatic outlet is as exhanst gas outlet; Descending pyrolysis reactor bottom access oil gas gas-solid separator; The oil gas vent of oil gas gas-solid separator connects the separation system in downstream, and solid outlet enters by the returning charge valve and burns the riser tube bottom.
2. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction 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 and be by diameter is that the big or small straight tube of riser tube gasifying reactor equivalent diameter different multiples is formed by connecting by the concentric reducer pipe fitting, and the diameter ratio of big or small straight tube is 1.2～2: 1.
3. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction device of stating, it is characterized in that burning riser tube bottom upwards 200mm-1500mm be returning charge mouth and the auxiliary coal fuel inlet 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.
4. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction device of stating, it is characterized in that hot grey gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, the optimal selection of the grey one-level gas-solid separator of heat is inertial separator, and the optimal selection of hot grey secondary gas-solid separator is vertical cyclone separator.
5. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction 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.
6. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction device of stating, it is characterized in that the oil gas gas-solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, optimal selection is vertical cyclone separator.
7. carry according to claim 1 the resinous shale downlink cycle fluidized bed pyrolysis liquefaction device of stating, it is characterized in that the oil shale gas solid separator is a kind of in vertical cyclone separator, horizontal cyclone separator, the inertial separator, optimal selection is inertial separator.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220525249 CN202912905U (en) | 2012-10-11 | 2012-10-11 | Pyrolysis liquefaction equipment of oil shale downward circulating fluid bed |
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| CN 201220525249 CN202912905U (en) | 2012-10-11 | 2012-10-11 | Pyrolysis liquefaction equipment of oil shale downward circulating fluid bed |
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| CN 201220525249 Expired - Lifetime CN202912905U (en) | 2012-10-11 | 2012-10-11 | Pyrolysis liquefaction equipment of oil shale downward circulating fluid bed |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102994136A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis liquification equipment of downstream circulating fluidized bed of oil shales |
| CN105907428A (en) * | 2016-04-29 | 2016-08-31 | 田原宇 | Small and medium sized fuel gas production device based on household refuse grading and flash pyrolysis and gasification |
| CN106118753A (en) * | 2016-04-29 | 2016-11-16 | 田原宇 | House refuse cleaning integrated gasification circulation cogeneration technique |
| CN106118754A (en) * | 2016-04-29 | 2016-11-16 | 田原宇 | House refuse cleaning integrated gasification circulation combined power generation device |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
| CN109666505A (en) * | 2017-10-16 | 2019-04-23 | 中国石油化工股份有限公司 | A kind of technique and system of catalytic pyrolysis |
| CN105779011B (en) * | 2016-04-29 | 2020-01-03 | 田原宇 | Process for preparing fuel gas by grading, fast pyrolysis and gasification of medium and small sized domestic garbage |
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2012
- 2012-10-11 CN CN 201220525249 patent/CN202912905U/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102994136A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Pyrolysis liquification equipment of downstream circulating fluidized bed of oil shales |
| CN105907428A (en) * | 2016-04-29 | 2016-08-31 | 田原宇 | Small and medium sized fuel gas production device based on household refuse grading and flash pyrolysis and gasification |
| CN106118753A (en) * | 2016-04-29 | 2016-11-16 | 田原宇 | House refuse cleaning integrated gasification circulation cogeneration technique |
| CN106118754A (en) * | 2016-04-29 | 2016-11-16 | 田原宇 | House refuse cleaning integrated gasification circulation combined power generation device |
| CN106118753B (en) * | 2016-04-29 | 2019-11-19 | 田原宇 | House refuse cleans integrated gasification and recycles cogeneration technique |
| CN106118754B (en) * | 2016-04-29 | 2019-11-19 | 田原宇 | House refuse cleans integrated gasification and recycles combined power generation device |
| CN105779011B (en) * | 2016-04-29 | 2020-01-03 | 田原宇 | Process for preparing fuel gas by grading, fast pyrolysis and gasification of medium and small sized domestic garbage |
| CN105907428B (en) * | 2016-04-29 | 2020-01-03 | 田原宇 | Device for preparing gas by grading, fast pyrolysis and gasification of small and medium-sized domestic garbage |
| CN109666505A (en) * | 2017-10-16 | 2019-04-23 | 中国石油化工股份有限公司 | A kind of technique and system of catalytic pyrolysis |
| CN109666505B (en) * | 2017-10-16 | 2021-06-11 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
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| C14 | Grant of patent or utility model | ||
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Assignee: Beijing news dtel Technology Co.,Ltd. Assignor: Tian Yuanyu Contract record no.: 2013110000050 Denomination of utility model: Pyrolysis liquification equipment of downstream circulating fluidized bed of oil shales Granted publication date: 20130501 License type: Exclusive License Record date: 20131009 |
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