CN205635484U - Oil shale pyrolysis system - Google Patents
Oil shale pyrolysis system Download PDFInfo
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- CN205635484U CN205635484U CN201620246473.4U CN201620246473U CN205635484U CN 205635484 U CN205635484 U CN 205635484U CN 201620246473 U CN201620246473 U CN 201620246473U CN 205635484 U CN205635484 U CN 205635484U
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- pyrolysis
- reactor
- oil shale
- oil
- hopper
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Abstract
The utility model relates to an oil shale pyrolysis system, it includes oil shale hopper, microwave dryer, mechanical activation ware, pyrolysis hopper and removes bed pyrolytic reaction ware, wherein removes bed pyrolytic reaction ware and includes: the oil shale entry is located the top of reactor, the export of pyrolysis oil gas is located on the roof and/or lateral wall of reactor, semi -coke outlet is located the bottom of reactor, regenerative radiant tube the inside of removing bed pyrolytic reaction ware along the direction of height multilayer of reactor arranges, every layer has many parallel regenerative radiant tube each other on the horizontal direction, wherein, oil shale hopper, microwave dryer, mechanical activation ware and pyrolysis hopper communicate in proper order, the pyrolysis hopper with the oil shale entry that removes bed pyrolytic reaction ware is linked together. The utility model provides the high utilization ratio of raw materials for the reaction rate, and can obtain the higher pyrolysis oil of quality.
Description
Technical field
This utility model generally relates to pyrolysis system, is specifically related to a kind of oil shale pyrolysis system.
Background technology
The oil shale resources of China are enriched, and be converted into shale oil there are about if having verified oil shale reserves
More than 400 hundred million tons.Currently, for the countries such as China, the crude oil of production can not meet this country
Demand, it is necessary to rely on substantial amounts of imported crude oil.This not only involves the national economic development, also relation
To national energy security problem.In the face of petroleum resources in short supply, shale oil industry should be advised energetically
Draw development.
Carbonization furnace can be divided into massive shale gas retort (oil shale granularity typically at 8mm or
More than 10mm), granule and powder carbonization furnace.China's shale oil yield is constantly increasing every year
Long, but the oily yield that the domestic dry distilling type of furnace can only be used for being pyrolyzed massive shale and device is relatively low,
Causing little granule shale to make full use of, oil shale utilization rate is the highest, and due to gas as heat
Carrier, carbonization gas is rushed dilute, and its condensate recovery system is huge, and gas heating value is low, it is difficult to further
Comprehensive utilization.And the most ripe Oil Shale Particles retorting technique mostly is solid thermal carriers and directly heats
, there is complex process operation link too many, the shortcomings such as manufacturing cost is high in raw material.Additionally, at present
Oil shale retorting technology is all not provided with pre-activate device, there is pyrolysis oil heavier, and molecular weight is bigger
Problem.
Fig. 1 is the oil shale pyrolysis process chart of prior art one.This system includes: 1, add
Material equipment；2, gas collects umbrella；3, body of heater；4, retort section；5, mixing chamber；6, arch abutment；7、
Circulating air entrance；8, gasification section；9, public attention；10, ash ejector；11, cupel；12, water seal.
It is upright that this China's Fushun stove is oil shale retorting and oil shale semi-coke gasification links together
Cylinder type stove, top is retort section, and bottom is gasification section.The raw material shale of 8-75mm, from dry
Furnace top loads machine and adds in stove, is dried, dry distilling in the retort section on stove top.After dry distilling
Shale semicockes i.e. enter the gasification section below retort section, in the heat of gasification section shale semicockes Yu rising
Main air meets, and carries out the combustion reaction of fierceness, forms the oxide layer of high temperature.The temperature of oxide layer exists
About 800-1000 DEG C, semicoke is become shale ashes after being aoxidized by oxide layer and discharges out of the furnace.Gasification section
Generation gas then enter retort section, heat raw shale oil.The dry distilling oil gas of gas retort outlet, warp
After crossing a series of condensation, cooling and shale oil recovery, a gained gas part send heat accumulating type to heat
Stove heats, as gas retort circulating air；A part is as the fuel of recuperative heater；Surplus
Remaining part is divided, and is sent to boiler and makees fuel.
The shortcoming of prior art one is: be not provided with mechanical activation device, and pyrolysis oil is heavier, and quality is low；
Stove bottom, Fushun, owing to entering air, has surplus air and enters retort section, burns part oil
Gas, causes oil yield low；Adding substantial amounts of air in stove, contained nitrogen has rushed carbonization gas dilute, fall
The low calorific value of gas, and cause condensate recovery system and equipment huge, cooling water amount is too many；
Can only dry distilling bulk oil shale, oil shale utilization rate is low.
Fig. 2 is the oil shale pyrolysis process chart of prior art two.This technique doing oil shale
Dry, pyrolysis and three technological processes of burning of shale semicockes complete in being integrated into a swinging stove.
This stove is the swinging kiln of horizontal tilt.A diameter of 8.2m of day processing 6000t oil shale stove,
Long 62.5m.Oil shale raw material enters gas retort, and drying section is indirectly heated dry by heat smoke
Dry, dried oil shale enters pyrolysis (dry distilling) section, with the hot shale ashes from burning zone
(750 DEG C) mix mutually and are heated to about 500 DEG C, and shale pyrolysis generates shale oil, gas and semicoke.
Oil gas is derived, condensation generates shale oil and high heating value carbonization gas.Semicoke (with shale ashes) then enters combustion
Burning section, meeting air burning also becomes shale ashes, and about 800 DEG C, the hot shale ashes of part are by outside stove
A piece serpentine pipe input retort section in face heats dry rectificating oil shale as solid thermal carriers, and formation follows
Ring utilizes；Cooled section of the hot shale ashes of another part are transported comes out of the stove.
The shortcoming of prior art two is: three technological processes realize in being integrated into a rotary furnace, work
Process flow too complex, long-time properly functioning relatively difficult；Equipment is huge, and structure is complicated, dimension
The amount of repairing is big, and operating cost is high.
Fig. 3 is the oil shale pyrolysis process chart of prior art three.This technology utilization heat smoke pair
Oil shale particle raw material is dried, and uses the high-temperature flue gas that semicoke or carbonization gas burning produce to dry
Dry oil shale particle heats indirectly to realize pyrolysis, obtains high-temperature oil gas and semicoke.To high temperature
Oil gas carries out filtering and after heat exchange, carrying out fractional distillation and obtain gasoline, diesel oil, heavy oil and carbonization gas.
The shortcoming of prior art three is: raw shale oil granule is less, in the accumulation of dry distilling indoor more
Densification, pyrolysis oil gas in dry distilling indoor can not be derived in time, and second pyrolysis easily occurs, and oil yield is not
High；Oil shale piles up densification, poor fluidity in reactor, is difficult to discharge；It is not provided with machinery to live
Gasifying device, pyrolysis oil is heavier, and quality is low.
Therefore, in order to improve the utilization rate of raw material, improve the thermal efficiency of heating burning, obtain quality
Higher pyrolysis oil, it is necessary to propose a kind of new oil shale pyrolysis system.
Utility model content
The purpose of this utility model is to provide a kind of oil shale pyrolysis system, mainly passes through microwave drying
The coal heat accumulating type down-flow fluidized bed using ECT fast pyrogenation of mechanical activation, obtains the pyrolysis oil that quality is higher in advance.
This utility model provides a kind of oil shale pyrolysis system, and it includes oil shale hopper, microwave
Exsiccator, mechanical activation device, pyrolysis hopper and moving bed pyrolysis reactor, wherein moving bed pyrolysis is anti-
Device is answered to include:
Oil shale entrance, described oil shale entrance is positioned at the top of described reactor；
Pyrolysis oil gas vent, described pyrolysis oil gas vent is positioned at roof and/or the sidewall of described reactor
On；
Semicoke exports, and the outlet of described semicoke is positioned at the bottom of described reactor；
Heat accumulation type radiant tube, described heat accumulation type radiant tube is on the edge, inside of described moving bed pyrolysis reactor
The short transverse multi-tier arrangement of described reactor, every layer have much the most parallel to each other
Heat accumulation type radiant tube；
Wherein, described oil shale hopper, microwave dryer, mechanical activation device and pyrolysis hopper connect successively
Logical, described pyrolysis hopper is connected with the oil shale entrance of described moving bed pyrolysis reactor.
Above-mentioned system, described mechanical activation device is ball mill.
Above-mentioned system, also includes the second feeding screw, described second feeding screw respectively with institute
The outlet stating pyrolysis hopper is connected with the oil shale entrance of described pyrolysis reactor.
Above-mentioned system, also includes the first feeding screw, described first feeding screw respectively with institute
The outlet stating oil shale hopper is connected with the entrance of described microwave dryer.
Above-mentioned system, described system also includes being pyrolyzed cyclone separator, filter and fractionating column, institute
State pyrolysis cyclone separator respectively with pyrolysis oil gas vent and the described filter of described pyrolysis reactor
Entrance is connected, and the outlet of described filter is connected with the entrance of described fractionating column.
Above-mentioned system, also includes fuel cartridge, the gas outlet of described fractionating column and described fuel cartridge phase
Connection.
Or, above-mentioned system, the entrance of described fractionating column and the pyrolysis oil gas vent of described reactor
Being connected, the gas outlet of described fractionating column is connected with described fuel cartridge.
Above-mentioned system, also includes gasification furnace, and described gasification furnace is by conveying worm and described pyrolysis
The semicoke outlet of reactor is connected.
Above-mentioned system, described system also includes combustible gas passage, and described combustible gas passage is by described gas
Change stove to be connected with the combustible gas entrance of the heat accumulation type radiant tube of described pyrolysis reactor.
The beneficial effects of the utility model are, this kind of oil shale pyrolysis system, take heat accumulating type to radiate
Pipe down-flow fluidized bed using ECT technique heating powder oil shale, uniformity of temperature profile, heats is good, can realize material
Fast pyrogenation, hydrocarbon yield is high.This system applied microwave dry technology, rate of drying is fast, efficiency
Height, uniform drying, it is achieved that energy-conservation, cleaning produces, and easily is automated control.This system
Also oil shale is carried out mechanical activation in advance, has added the chemical reactivity of oil shale, reduce
Temperature required for pyrolytic reaction, thus pyrolytic tar is relatively light, quality better, petrol and diesel oil fraction is high.Whole
For body, the pyrolysis oven operation temperature of this system is low, and energy consumption is low, and is prone to the regular maintenance of device.
Accompanying drawing explanation
Fig. 1 is the oil shale pyrolysis process chart of prior art one；
Fig. 2 is the oil shale pyrolysis process chart of prior art two；
Fig. 3 is the oil shale pyrolysis process chart of prior art three；And
Fig. 4 is oil shale pyrolysis process chart of the present utility model.
Detailed description of the invention
Below in conjunction with drawings and Examples, detailed description of the invention of the present utility model is carried out more detailed
Thin explanation, so as to be more fully understood that the excellent of scheme of the present utility model and its various aspects
Point.But, specific embodiments described below and embodiment be only descriptive purpose rather than
To restriction of the present utility model.
As shown in Figure 4, a kind of oil shale pyrolysis system flow chart of this utility model embodiment, should
Heat accumulating type down-flow fluidized bed using ECT pyrolysis system includes: 1. loading hopper；2. microwave dryer；3. heat accumulating type is descending
Bed reactor；4. ball mill (mechanical activation device) is 5. pyrolyzed hopper；6. feeding screw；7.
Pyrolysis cyclone separator；8. filter；9. fractionating column；10. combustion gas air-introduced machine；11. fuel cartridges；
12. combustion gas pressure fan；13. gasification furnaces；14. conveying worms.
Loading hopper 1 is connected to microwave dryer 2 entrance by feed arrangement, and microwave dryer 2 goes out
Mouth is connected with ball mill 4 entrance.
Ball mill 4 outlet is connected with pyrolysis hopper 5 entrance, and pyrolysis hopper outlet is entered by spiral
Glassware 6 is connected to the feeding mouth of heat accumulating type descending-bed reactor 3.
Descending-bed reactor 3 includes upper feed inlet, combustion gas, air intake and oil gas, flue gas,
Semicoke exports.
Oil gas vent is connected with one-level pyrolysis cyclone separator 7 entrance, two grades of pyrolysis cyclone separator
The gas outlet of 7 is connected with filter 8 entrance；Filter 8 outlet is connected with fractionating column 9 entrance,
Fractionating column 9 gas outlet is connected with combustion gas air-introduced machine 10 entrance；Combustion gas air-introduced machine 10 exports and combustion gas
Tank 11 entrance connects, and fuel cartridge 11 outlet is connected with combustion gas pressure fan 12 entrance；Combustion gas is blown
Machine 12 outlet is connected with the fuel gas inlet of descending-bed reactor 3.
Descending-bed reactor 3 semicoke exit design, in bottom, is connected to entering of conveying worm 14
Mouthful；Two grades of pyrolysis cyclone separator 7 discharging openings are connected with the entrance of conveying worm 14；Spiral shell
The outlet of rotation conveyer 14 is connected with gasification furnace 13 entrance；The gas outlet of gasification furnace 13 with under
The fuel gas inlet of row bed reactor 3 is connected.
Heat accumulating type down-flow fluidized bed using ECT pyrolytic process of the present utility model includes:
(1) Oil Shale Particles being crushed to granularity≤20mm enters microwave drying by loading hopper 1
Device 2, in microwave dryer, oil shale by quick, enter into ball mill 4 after drying uniformly
In carry out mechanical activation, some equipped with ball-milling medium steel ball in ball mill, by stirring motor drive rotation
Turn, in rotary course steel ball oil shale rubbed, collide, impact, the machinery masterpiece such as shearing
With, adding the chemism of oil shale, the mechanical activation time controls in the range of 10min-2h.
Powder oil shale through mechanical activation enters in pyrolysis hopper 5.
(2) to enter heat accumulating type down-flow fluidized bed using ECT through feeding screw 6 anti-in pyrolysis hopper 5 for oil shale
Answer device 3, heat accumulating type descending-bed reactor has been evenly arranged unidirectional heat accumulation type radiant tube, tube wall
Temperature utilizes gas control valve to control 400-700 DEG C of scope, oil shale in the reactor from upper and
Lower stop 5s-5min, and it is heated to 400-600 DEG C, complete pyrolytic process.
(3) oil gas that pyrolysis produces is discharged from reactor and to pass through two stage cyclone separator 7 laggard
Enter in filter 8 and filter, oil gas after filtration enter fractionating column 9 fractional distillation obtain gasoline, diesel oil and
Heavy oil, after fractional distillation, remaining carbonization gas sends into fuel cartridge 11, carbonization gas warp through combustion gas blower fan 10
The radiation of pyrolysis reactor 3 is sent into gasification furnace 13 together with the combustible gas that combustion gas pressure fan 12 produces
Pipe fuel gas inlet.
(4) powder that the semicoke that oil shale pyrolysis produces separates with two stage cyclone separator 7
Semicoke sends into gasification furnace 13 by conveying worm 14 together, and the lime-ash after gasification is discharged.
This system applied microwave dry technology, is molecular motion energy by microwave energy, and with heat
Form show, make water temperature raise and leave material, so that material is dried.
In traditional drying process, for improving rate of drying, need elevated external temperatures, strengthen temperature difference ladder
Degree, but the most easily produce the phenomenon that material is scorched outside and underdone inside.But when using microwave heating, no matter
Material shapes is how, heat can uniformly penetrating, and expansion effect can be produced, be beneficial to pulverize.Cause
Microwave energy penetrates material and directly heats, and the polar molecule in material is very fast shake under the effect of microwave field
Swinging, improve the activation energy of chemical reaction, accelerate response speed, uniform drying, efficiency is high,
Achieve energy-conservation, cleaning production, and easily be automated control.
This system can also carry out mechanical activation in advance to oil shale, and mechanical activation refers to solid matter
Rubbing, collide, impact, under the mechanical force such as shearing, make crystal structure and physical and chemical performance send out
Raw change, makes some mechanical can be transformed into the interior energy of material, thus causes the chemism of solid to increase
Adding, oil shale chemistry increased activity, granule chemical energy increases, and improves the chemical reaction of oil shale
Activity, the temperature required for pyrolytic reaction reduces, thus pyrolytic tar is relatively light, quality better.Machinery
Oil shale after activation enters in heat accumulating type fast pyrogenation reaction unit, can be a large amount of through fast pyrogenation
Extract oil gas product.
Embodiment
Utilize heat accumulating type down-flow fluidized bed using ECT pyrolysis system of the present utility model that Longkou oil shale is processed,
The basic data of raw material, process operation parameter and material balance are shown in Table 1-table 2.
Table 1: Longkou oil shale basic data
M in table 1adRepresent air-dried moisture；AdRepresent and be dried base ash；VadRepresent air-dried basis volatilization
Point；
Table 2: process operation parameter
| Sequence number | Parameter name | Parameter value | Sequence number | Parameter name | Parameter value |
| 1 | Top radial canal wall surface temperature | 500℃ | Reactor lower part temperature | 450℃ | |
| 2 | Middle part radial canal wall surface temperature | 500℃ | Reactor outlet temperature | 440℃ | |
| 3 | Lower radiant tube wall surface temperature | 470℃ | Whirlwind outlet temperature | 425℃ | |
| 4 | Reactor upper temp | 425℃ | Reactor pressure | 1.8Kpa | |
| 5 | Reactor middle portion temperature | 450℃ |
Utilize the pyrolysis oil property that this system prepares: pyrolysis oil density is 0.89g cm-3, density
Relatively low, oil product is lighter.Pyrolysis oil product being simulated distillation obtain, gasoline fraction accounts for 15%, bavin
Oil distillate accounts for 55%, and petrol and diesel oil ends content is high.
Last it is noted that obvious, above-described embodiment is only new for clearly demonstrating this practicality
Type example, and not restriction to embodiment.Ordinary skill people for art
For Yuan, can also make other changes in different forms on the basis of the above description.
Here without also cannot all of embodiment be given exhaustive.And thus amplified out aobvious and easy
The change seen or variation still in protection domain of the present utility model among.
Claims (9)
1. an oil shale pyrolysis system, it is characterised in that described system includes oil shale hopper, microwave dryer, mechanical activation device, pyrolysis hopper and moving bed pyrolysis reactor,
Wherein moving bed pyrolysis reactor includes:
Oil shale entrance, described oil shale entrance is positioned at the top of described reactor；
Pyrolysis oil gas vent, described pyrolysis oil gas vent is positioned on roof and/or the sidewall of described reactor；
Semicoke exports, and the outlet of described semicoke is positioned at the bottom of described reactor；
Heat accumulation type radiant tube, described heat accumulation type radiant tube is in the inside of described moving bed pyrolysis reactor along the short transverse multi-tier arrangement of described reactor, and every layer has many heat accumulation type radiant tubes the most parallel to each other；
Wherein, described oil shale hopper, microwave dryer, mechanical activation device and pyrolysis hopper are sequentially communicated, and described pyrolysis hopper is connected with the oil shale entrance of described moving bed pyrolysis reactor.
System the most according to claim 1, it is characterised in that described mechanical activation device is ball mill.
System the most according to claim 1, it is characterised in that described system also includes the second feeding screw, described second feeding screw is connected with the outlet of described pyrolysis hopper and the oil shale entrance of described pyrolysis reactor respectively.
System the most according to claim 1, it is characterised in that described system also includes the first feeding screw, described first feeding screw is connected with the outlet of described oil shale hopper and the entrance of described microwave dryer respectively.
System the most according to claim 1, it is characterized in that, described system also includes being pyrolyzed cyclone separator, filter and fractionating column, described pyrolysis cyclone separator is connected with the pyrolysis oil gas vent of described pyrolysis reactor and the entrance of described filter respectively, and the outlet of described filter is connected with the entrance of described fractionating column.
6. according to the system described in claim 5, it is characterised in that described system also includes that fuel cartridge, the gas outlet of described fractionating column are connected with described fuel cartridge.
The most according to claim 1 or 5, system, it is characterised in that described system also includes gasification furnace, described gasification furnace is connected with the semicoke outlet of described pyrolysis reactor by conveying worm.
System the most according to claim 7, it is characterised in that described system also includes that described gasification furnace is connected by combustible gas passage, described combustible gas passage with the combustible gas entrance of the heat accumulation type radiant tube of described pyrolysis reactor.
System the most according to claim 1, it is characterised in that described system also includes that fractionating column and fuel cartridge, the entrance of described fractionating column are connected with the pyrolysis oil gas vent of described reactor, and the gas outlet of described fractionating column is connected with described fuel cartridge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620246473.4U CN205635484U (en) | 2016-03-28 | 2016-03-28 | Oil shale pyrolysis system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620246473.4U CN205635484U (en) | 2016-03-28 | 2016-03-28 | Oil shale pyrolysis system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205635484U true CN205635484U (en) | 2016-10-12 |
Family
ID=57074260
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620246473.4U Expired - Fee Related CN205635484U (en) | 2016-03-28 | 2016-03-28 | Oil shale pyrolysis system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205635484U (en) |
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2016
- 2016-03-28 CN CN201620246473.4U patent/CN205635484U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Oil shale pyrolysis system Effective date of registration: 20180327 Granted publication date: 20161012 Pledgee: Tianfeng Securities Co.,Ltd. Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000230 |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20190121 Granted publication date: 20161012 |
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| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20220921 Granted publication date: 20161012 |
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| PD01 | Discharge of preservation of patent | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20161012 |
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| CF01 | Termination of patent right due to non-payment of annual fee |