CN102851048B - A kind of gas purge system realizing slag heat utilization - Google Patents
A kind of gas purge system realizing slag heat utilization Download PDFInfo
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- CN102851048B CN102851048B CN201210315332.XA CN201210315332A CN102851048B CN 102851048 B CN102851048 B CN 102851048B CN 201210315332 A CN201210315332 A CN 201210315332A CN 102851048 B CN102851048 B CN 102851048B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of gas purge system realizing slag heat utilization.This gas purge system includes the reaction generating means for producing dusty gas and discharges, with the dusty gas on this reaction generating means, the gas dust-removing device that end is connected, this gas dust-removing device is provided with slag-draining device, it is provided with heat-exchange system between described reaction generating means and gas dust-removing device, this heat-exchange system includes the first flow path through an exchanger heat exchange connection and second flow path, described first flow path is the raw materials passage of reaction generating means, second flow path is the slag charge slagging channel of gas dust-removing device, and this slagging channel is connected with described slag-draining device.This gas purge system can will enter the raw material of this reaction generating means with the slag charge preheating of gas dust-removing device, saves the energy.
Description
Technical field
The present invention relates to a kind of gas purge system realizing slag heat utilization.
Background technology
Oil shale retorting is divided into underground retoring (underground retorting) and dry distilling on the ground (upground retorting)
Two kinds.Wherein, though underground retoring technology is applied for a patent by Shell Co. Ltd, but still in development, there is no industrial applications.
Dry distilling on the ground is still the main path that oil shale develops.Oil shale dry distilling on the ground is divided into again external-heat dry distilling and internal heat type dry distilling
Two kinds.External-heat dry distilling refers to that the oil shale that heat carrier is heated in stove by furnace wall carries out dry distilling, and this technology is eliminated the most；
Internal heat type dry distilling refers to that heat carrier directly contacts with oil shale in stove, carries out dry distilling, is the main flow skill of current oil shale exploitation
Art.The heat carrier of internal heat type dry distilling is divided into gas heat carrier and solid thermal carriers.In general, either in gas heat carrier
Hot type dry distilling liquefaction system, or solid thermal carriers internal heat type dry distilling liquefaction system, all include that dry distillation reactor device and condensation are reclaimed
System.Dry distillation reactor device is defined as that oil shale is carried out dry distilling hot-working and produces dry distilling product and outwards discharge this by the application
The device of dry distilling product, is defined as the system that dry distilling product is condensed and reclaimed by condensate recovery system.
For gas heat carrier internal heat type dry distilling liquefaction system, it is directly entered cold from the dry distilling product of dry distillation reactor device release
Condensation reclaiming system.Wherein, most typical gas heat carrier internal heat type dry distilling liquefaction system has Chinese Fushun formula system, Brazil pendant spy
Luo Sekesi (Petrosix) system, Estonia's Abel Kiviat (Kiviter) system etc..Solid thermal carriers internal heat type is done
For evaporating liquefaction system, the material owing to discharging from dry distillation reactor device is by the page making the shale ashes of solid thermal carriers, generation
Rock semicoke and dry distilling product mix, and are currently gaseous state by the dust removal with machine equipment such as gravitational precipitator, cyclone separator
Shale ashes and the shale semicockes of dry distilling product and solid separate, then dry distilling product is imported condensate recovery system, and separates
The mixture of shale ashes and shale semicockes then burns so that it is temperature reaches about 800 DEG C, more again as dry rectificating oil shale
Solid thermal carriers.Wherein, most typical solid thermal carriers internal heat type dry distilling liquefaction system has Estonian Ge Luote (Galoter)
System, Ta Seke (Taciuk) system (also known as ATP) etc. of Australia.
In a word, no matter gas heat carrier internal heat type dry distilling liquefaction system or solid thermal carriers internal heat type dry distilling liquefaction system, dry distilling
All with a certain amount of dust during product entrance condensate recovery system.For gas heat carrier internal heat type dry distilling liquefaction system,
Source of Dust is mainly the solid matter being carried over dry distillation reactor device with air-flow；For solid thermal carriers internal heat types dry distilling liquefaction system
For system, the solid matter that Source of Dust is not mainly separated by dust removal with machine equipment.Gas heat carrier internal heat type dry distilling system
In oil system, the dust that dry distilling product is carried when entering condensate recovery system is more, can generate larger amount of greasy filth.Comparatively speaking
The greasy filth amount of gas heat carrier internal heat type dry distilling liquefaction system is less.Greasy filth is the mixture of water, shale oil and dust.Air heat
In the greasy filth that carrier internal heat type dry distilling liquefaction system is generated, shale oil accounts for about 30%, and dust accounts for about 20%.If greasy filth obtains not
To processing in time, not only cause oil loss, and affect production.The main path reducing greasy filth at present is that reinforcement entrance dry distilling is anti-
The screening answering the oil shale of device, the distribution improving oil shale, the air flow method improved in dry distillation reactor device and heat supply ratio with
And reduce the outlet temperature of dry distillation reactor device.Wherein, the outlet temperature purpose reducing dry distillation reactor device is to make dry distillation reactor fill
The warm and humid bed of material is formed on the top put, thus reduces the discharge of dust.
Visible, prior art teaches undoubtedly and reduces greasy filth generation by the outlet temperature reducing dry distillation reactor device.Phase therewith
The interesting fact answered is, in current gas heat carrier internal heat type dry distilling liquefaction system, and the outlet temperature of dry distillation reactor device
The most relatively low, in China's Fushun formula system, the outlet temperature of dry distillation reactor device is 80 to 100 DEG C, Brazil pendant spy as previously mentioned
The outlet temperature of Luo Sekesi (Petrosix) system is about 150 DEG C.Shale oil is commonly divided into mink cell focus, middle matter oil and light
Matter oil.The division of mink cell focus, middle matter oil and light oil is the strictest.The application by boiling point more than 450 DEG C part definition attach most importance to
Matter oil, matter oil, the just boiling point part definition between 40 to 179 DEG C during boiling point part between 180 to 449 DEG C is defined as
For light oil.Owing in current gas heat carrier internal heat type dry distilling liquefaction system, the outlet temperature of dry distillation reactor device is relatively low, therefore
The shale oil being recovered to from condensate recovery system is mink cell focus, middle matter oil and light oil mixture.This is just for the follow-up profit of shale oil
With making troubles.Solid thermal carriers internal heat type dry distilling liquefaction system equally exists such problem.
Summary of the invention
<Part I>
First technical problem that the application aims to solve the problem that is to provide a kind of oil shale retorting liquefaction system reducing greasy filth yield.
To this end, the oil shale retorting liquefaction system of the application includes dry distillation reactor device and condensate recovery system, described dry distillation reactor
It is connected by dedusting system between dry distilling product release end and the dry distilling product receiving terminal of condensate recovery system of device, this gas
Body dust pelletizing system at least includes that the first gas purification units, described first gas purification units use filtering accuracy 0.01 to 80
The porous filter material of micron is filter element.Porous filter material intercepts the solids in gas except the main material that passes through itself
Thus reach to filter outside purpose, in filter process, less solids also can be formed at material surface and put up a bridge, thus set up
Less cavity is to increase the interception result to solids.It addition, porous filter material also has gravitational settling, inertial collision concurrently
Deng the mode of trapping solid particle, further increase filter effect.Therefore, use filtering accuracy at above-mentioned interval model before condensation
Enclosing after dry distilling product implemented to purify by interior porous filter material, the dust content in dry distilling product can be greatly reduced, thus substantially
Reduce the yield of follow-up greasy filth.This is that dust removal with machine, electrostatic precipitation are unapproachable.
Through measuring and calculating, when the first gas purification units uses filtering accuracy porous filter material below 10 microns to be filter element
Time, due to higher filtering accuracy, the dust content in dry distilling product after dedusting system processes at least can be reduced to
5mg/m3Below.At this moment, the liquid substance that the product that condensation obtains mainly is made up of shale oil and water, there is not oil
Mud composition.This provides condition for the technological process simplifying condensate recovery system, also can improve the productivity of shale oil simultaneously.And incite somebody to action
The filtering accuracy of porous filter material controls to can ensure that again higher filter efficiency more than 0.1 micron.Based on such reason,
It was filtering element that the first gas purification units in the application preferably employs filtering accuracy at the porous filter material of 0.1 to 10 micron
Part.
In the case of the Dust Capacity that need to process in dedusting system is relatively big, in order to avoid to the first frequent blowback of gas purification units
Regeneration, described dedusting system also includes that the second gas being arranged on the first gas purification units front end by udst separation direction is clean
Changing unit, described second gas purification units uses one or both in mechanical dust collector and electrostatic precipitator.Second gas is clean
Changing unit and the dry distilling product having just enter into dedusting system can carry out one-level or what purified treatment, remove in dry distilling product is big
The dust of part, makes the Dust Capacity in entrance the first gas purification units to be greatly reduced, thus improves the first gas purification units
The time of continuous firing, reduce blowback frequency.
For the slag charge waste heat utilizing dedusting system to trap, set between described dry distillation reactor device and gas dust pelletizing system
Having heat-exchange system, this heat-exchange system includes the first flow path through an exchanger heat exchange connection and second flow path, described first flow path
For the oil shale loading channel of dry distillation reactor device, second flow path is the slag charge slagging channel of dedusting system.For existing
For gas heat carrier internal heat type dry distilling liquefaction system, due to be not provided with between dry distillation reactor device and condensate recovery system for
The equipment of dust in trapping dry distilling product, is also impossible to utilize the dust heat trapped to entering dry distillation reactor device
Oil shale preheat.For existing solid thermal carriers internal heat type dry distilling liquefaction system, trap be shale ashes and
The mixture of shale semicockes, this mixture must burn after as solid thermal carriers, be the most also difficult to this mixture directly to i.e.
The oil shale entering dry distillation reactor device is preheated.In a word, the above-mentioned this UTILIZATION OF VESIDUAL HEAT IN mode of the application is skillfully constructed, energy
Enough waste heats to the slag charge that dedusting system traps effectively utilize.
The application background technology is mentioned, owing to the outlet temperature of dry distillation reactor device is relatively low, is recovered to from condensate recovery system
Shale oil is mink cell focus, middle matter oil and light oil mixture, thus the utilization for shale oil is made troubles.To this, remove at gas
In the range of dirt system can be born (within the temperature range of in the mainly first gas purification units, porous filter material can tolerate) to the greatest extent
The possible outlet temperature improving dry distillation reactor device becomes the direction that the application is considered.And above-mentioned slag charge UTILIZATION OF VESIDUAL HEAT IN mode
It it is exactly the application important channel of improving dry distillation reactor device outlet temperature.The concrete scheme of the application is: described dry distilling product is released
Put the outlet temperature of end guarantee to make the filter element in the first gas purification units can its porous filter material tolerable 400 to
Filter in the temperature range of 800 DEG C；Further, described condensate recovery system has entering from described dry distilling product receiving terminal
The dry distilling product of inlet temperature >=350 DEG C and ＜ 800 DEG C condenses the system of recovery step by step.The program actually to guarantee
Porous filter material works in the temperature range of 400 to 800 DEG C, make dry distilling product receiving terminal inlet temperature energy >=350 DEG C and
＜ 800 DEG C, in order in follow-up condensation removal process, mink cell focus, middle matter oil are separated with light oil.
Just work in the temperature range of 400 to 800 DEG C due to porous filter material, also therefore be able to from dedusting system
Discharge the slag charge of high temperature.Even if calculating by the heat exchange efficiency of 50%, the oil shale that will enter dry distillation reactor device the most also can
It is heated to about 200 DEG C, thus by the surface water of oil shale with combine water and be reduced to about 2%.So, after being preheated
After oil shale enters dry distillation reactor device, it becomes possible to guarantee from the dry distilling product that dry distilling product release end discharge outlet temperature is higher.
So circulation, oil shale retorting liquefaction system is up to and maintains a stable running status.
Certainly, the filter element in described first gas purification units preferably can be carried out in the temperature range of 500 to 800 DEG C
Filter；And inlet temperature >=450 DEG C of described dry distilling product receiving terminal and ＜ 800 DEG C.So, additionally it is possible at least divide from shale oil
Go out the middle matter oil of a part.
The oil shale retorting liquefaction system of the application the most further provides the heat exchanger that a kind of heat exchange efficiency is higher.Specifically,
This heat exchanger includes inner core and the urceolus being coaxially disposed, and described inner core is rotatable and urceolus is fixed, when inner core rotates, and oil shale
Oil shale charging aperture from inner core enters the cylinder of inner core and gradually flows to the oil shale discharging opening on inner core, and slag charge is then from outward
Slag charge charging aperture on cylinder enters between urceolus and inner core and gradually flows to the slag charge discharging opening on urceolus.Urceolus can be the most anti-
Only the heat of slag charge is to the outside diffusion of heat exchanger, and the inner core of rotation can make oil shale therein be heated evenly, urceolus and the length of inner core
Degree ensure that enough heat-exchange times.Therefore, the high efficient heat exchanging that this heat exchanger is capable of between solid and solid.Compare
Saying, this exchanger heat conductance is higher, and the heat-transfer effect of whole process is more preferable.
Wherein, described oil shale charging aperture and slag charge charging aperture are preferably located at the same side of heat exchanger, described oil shale discharging opening and
Slag charge discharging opening is then positioned at the opposite side of heat exchanger, to be formed and to flow heat exchange.It addition, on the inner tube wall of described inner core and outer tube wall
Preferably further respectively have and promote with the rotation of inner core what the object in inner core and between inner core and urceolus moved to discharging direction to squeeze
Laminated structure, the most spiral helicine rib, blade etc..Like this, as long as oil page can be changed by adjusting the rotating speed of inner core
Rock and the slag charge time of staying in heat exchanger, in order to improve heat transfer effect according to specific needs.Certainly, if be not provided with completely
Above-mentioned extrusion structure or only setting are positioned at the extrusion structure on inner core inner tube wall, it is possible to by overall to inner core and urceolus to discharging direction
Tilt certain angle (being preferably set for 10 to 30 °), in order to rely on gravity to make material flow voluntarily.
In sum, the oil shale retorting liquefaction system of the application produces during condensation removal process on the one hand can be decreased or even eliminated
Greasy filth, on the one hand can improve the outlet temperature of dry distillation reactor device under energy saving condition so that shale oil is segmented recovery,
Compared to prior art, there is marked improvement, be particularly suitable as gas heat carrier internal heat type dry distilling liquefaction system.
<Part II>
Second technical problem that the application aims to solve the problem that is to provide a kind of oil shale retorting system making shale oil be segmented recovery
Oil method.The description below of this " Part II " can refer to the content of " Part I " and understands.
To this end, the step that the oil shale retorting method for producing oil of the application includes is: one, release from the dry distilling product of dry distillation reactor device
Put end discharge dry distilling product and be passed through dedusting system；Two, the dry distilling after obtaining slag charge and purifying is processed through dedusting system
Product, described slag charge leads to heat-exchange system, and the dry distilling product after described purification leads to condensate recovery system；Three, described slag charge exists
The oil shale that will enter dry distillation reactor device is heated by heat-exchange system, dry in entrance to guarantee the oil shale after this heating
Discharging, from dry distilling product, the dry distilling product that end discharge outlet temperature is higher after evaporating reaction unit reaction, this outlet temperature guarantees to make dry distilling
Product dry distilling product receiving terminal at condensate recovery system after dedusting system still reaches >=the entrance temperature of 350 DEG C and ＜ 800 DEG C
Degree；Four, by condensate recovery system, the dry distilling product entered from described dry distilling product receiving terminal is condensed recovery step by step.
Mentioning in above-mentioned " Part I ", the inlet temperature of dry distilling product receiving terminal is carried under energy saving condition by the method
High to >=350 DEG C and ＜ 800 DEG C, say, that compared with prior art, dry distilling product is condensed back proceeding by by the application
The temperature in time receiving improves more than 200 DEG C fully, therefore, just can obtain relatively thin in follow-up condensation removal process step by step
The shale oil divided.Based on alleged cause in above-mentioned " Part I ", the oil shale after being heated by heat-exchange system is being entered
The outlet temperature of the dry distilling product discharged from dry distilling product release end after entering dry distillation reactor device reaction can ensure that and makes this dry distilling product warp
Dedusting system reaches the >=inlet temperature of 450 DEG C and ＜ 800 DEG C at the dry distilling product receiving terminal of condensate recovery system after processing.
For the oil shale retorting method for producing oil of the application, dedusting system not necessarily uses the method for filtration.This is
Because in the oil shale retorting method for producing oil of the application, the primary effect of dedusting system is trapping dust, therefore, even if
Use traditional dust removal with machine device (such as gravitational precipitator or cyclone dust extractor) that such purpose can also be realized.Certainly,
The application still advises that described dedusting system at least includes that the first gas purification units, described first gas purification units use
Filtering accuracy is filter element at the porous filter material of 0.01 to 80 micron, and this filter element can be at its porous filter material
Tolerable 400(is preferably 500) filter to the temperature ranges of 800 DEG C.
Based on alleged cause in above-mentioned " Part I ", the situation that the Dust Capacity that need to process in dedusting system is bigger
Under, described dedusting system the most also includes the second gas being arranged on the first gas purification units front end by udst separation direction
Clean unit, described second gas purification units uses one or both in mechanical dust collector and electrostatic precipitator.The most permissible
Improve the time of the first gas purification units continuous firing, reduce blowback frequency.
Being equally based in above-mentioned " Part I " alleged cause, described first gas purification units uses filtering accuracy to exist
The porous filter material of 0.1 to 10 micron is filter element, in order to by the powder in the dry distilling product after dedusting system processes
Dust content is reduced to 5mg/m3Below.
As the concrete structure of heat-exchange system, described heat-exchange system includes through the first flow path and second that an exchanger heat exchange connects
Stream, described first flow path is the oil shale loading channel of dry distillation reactor device, and second flow path is the slag charge row of dedusting system
Slag passage.
Wherein, described heat exchanger includes inner core and the urceolus being coaxially disposed, and described inner core is rotatable and urceolus is fixed, when inner core turns
Time dynamic, oil shale oil shale charging aperture from inner core enters inner core cylinder and gradually flows to the oil shale discharging opening on inner core,
The slag charge then slag charge charging aperture from urceolus enters between urceolus and inner core and gradually flows to the slag charge discharging opening on urceolus.
Further, described oil shale charging aperture and slag charge charging aperture are respectively positioned on the same side of heat exchanger, described oil shale discharging
Mouth and slag charge discharging opening are respectively positioned on the opposite side of heat exchanger.
Further, the inner tube wall of described inner core and outer tube wall are respectively equipped with promote with the rotation of inner core in inner core and interior
The extrusion structure that object between cylinder and urceolus moves to discharging direction.
<Part III>
The 3rd technical problem that the application aims to solve the problem that is to provide a kind of gas purge system realizing slag heat utilization.This " the
Three parts " the description below can refer to the content of " Part II " and understand.
To this, this gas purge system include for produce dusty gas reaction generating means and with this reaction generating means
Dusty gas release end be connected gas dust-removing device, this gas dust-removing device is provided with slag-draining device, and described reaction fills
Put and be provided with heat-exchange system between gas dust-removing device, this heat-exchange system include through one exchanger heat exchange connect first flow path and
Second flow path, described first flow path is the raw materials passage of reaction generating means, and second flow path is the slag charge of gas dust-removing device
Slagging channel, this slagging channel is connected with described slag-draining device.
Further, described gas dust-removing device at least includes that the first gas purification units, described first gas purification units are adopted
It is filter element with filtering accuracy at the porous filter material of 0.01 to 100 micron.
Further, described first gas purification units uses the filtering accuracy at the porous filter material of 0.1 to 10 micron to be
Filtering element.
Wherein, described porous filter material is the highest can filter at 800 DEG C.
Further, described gas dust-removing device also includes being arranged on the first gas purification units front end by udst separation direction
Second gas purification units, described second gas purification units uses one or both in mechanical dust collector and electrostatic precipitator.
Further, described heat exchanger includes inner core and the urceolus being coaxially disposed, and described inner core is rotatable and urceolus is fixed, when
When inner core rotates, the raw material reacting generating means material inlet from inner core will be entered and enter inner core cylinder and gradually flow
Raw material discharging opening to inner core, the slag charge then slag charge charging aperture from urceolus discharged from gas dust-removing device enters urceolus with interior
Between Tong and gradually flow to the slag charge discharging opening on urceolus.
Further, described material inlet and slag charge charging aperture are respectively positioned on the same side of heat exchanger, described raw material discharging opening and
Slag charge discharging opening is respectively positioned on the opposite side of heat exchanger.
Further, the inner tube wall of described inner core and outer tube wall are respectively equipped with promote with the rotation of inner core in inner core and interior
The extrusion structure that material between cylinder and urceolus moves to discharging direction.
When described gas purge system is for oil shale retorting liquefaction, described reaction generating means is dry distillation reactor device, institute
The raw material stated is oil shale；Further, described filtering residue in heat-exchange system, the oil shale that will enter dry distillation reactor device is carried out
Heating, discharges end discharge outlet from described dusty gas with the oil shale after guaranteeing this heating after entering dry distillation reactor device reaction
The dry distilling product that temperature is higher, this outlet temperature guarantees to make dry distilling product still reach >=350 DEG C and ＜ after gas dust-removing device processes
The high temperature of 800 DEG C.
Further, the oil shale after being heated by heat-exchange system is discharged from dusty gas after entering dry distillation reactor device reaction
The outlet temperature of the dry distilling product that end is discharged can ensure that and makes this dry distilling product reach >=450 DEG C and ＜ after gas dust-removing device processes
The high temperature of 800 DEG C.
The present invention is described further with detailed description of the invention below in conjunction with the accompanying drawings.Aspect that the application adds and advantage will be
Giving out in the middle part of explained below, part will become apparent from the description below, or is recognized by the practice of the application.
Accompanying drawing explanation
Fig. 1 is the principle schematic (process chart) of the application oil shale retorting liquefaction system.
Fig. 2 is the structural representation of heat exchanger in the application oil shale retorting liquefaction system.
Detailed description of the invention
First combine accompanying drawing a kind of gas purge system realizing slag heat utilization of the application is specifically described.
As it is shown in figure 1, this gas purge system includes, for produce dusty gas reaction generating means 5 and with this reaction
The gas dust-removing device 6 that dusty gas release end on generating means 5 is connected, this gas dust-removing device 6 is provided with slag-draining device,
Being provided with heat-exchange system 4 between described reaction generating means 5 and gas dust-removing device 6, this heat-exchange system 4 includes through a heat exchanger
The first flow path 420 of 410 heat exchanges connections and second flow path 430, described first flow path 420 is the raw material of reaction generating means 5
Loading channel, second flow path 430 is the slag charge slagging channel of gas dust-removing device 6, this slagging channel and described slag-draining device phase
Even.Existing gas gas dust arrester 6 dust arrester 6 typically has with slag-draining device.Such as, gas dust-removing device 6
Bottom be typically the design of inverted cone, oral area has the valve for discharging.Some slag-draining devices are also possible to use more complicated machine
Tool, conventional has spiral discharging machine etc..Gas dust-removing device 6 can only with existing gravitational precipitator, cyclone dust extractor and
One or more in electrostatic precipitator.Described " first flow path 420 " and " second flow path 430 " refers to raw materials route
With slag charge deslagging route, reality generally includes one or more in conveyance conduit, conveyer belt." heat exchange connection " refers to first
Stream 420 and second flow path 430 can be directly realized by physics heat exchange.It is critical only that of this gas purge system can use dedusting
The slag charge preheating of device 6 will enter the raw material of this reaction generating means 5, saves the energy.
As it is shown in figure 1, in this gas purge system, described gas dust-removing device 6 at least includes the first gas purification units 210,
Described first gas purification units 210 uses filtering accuracy to be filter element at the porous filter material of 0.01 to 100 micron.For
Ensureing more higher filtering accuracy and higher filter efficiency, the first gas purification units 210 exists preferably with filtering accuracy
The porous filter material of 0.1 to 10 micron is filter element.If it addition, gas dust-removing device 6 will at high temperature work, institute
The porous filter material selected should the highest can filter at 800 DEG C.Meet such condition, selectable porous filtering
Material is mainly sintering diamond bit or ceramic porous material.Preferred FeAl intermetallic compound in sintering diamond bit
Porous material, TiAl intermetallic compound porous material or NiAl intermetallic compound porous material, this kind of material has higher
High temperature corrosion resistance, filtering accuracy and machinability, there is excellent comprehensive serviceability.On this basis, gas removes
Dirt device 6 also includes the second gas purification units 220 being arranged on the first gas purification units 210 front end by udst separation direction,
Described second gas purification units 220 uses one or both in mechanical dust collector and electrostatic precipitator.By the first gas purification
Unit 210 and the second gas purification units 220 collocation get up using effect more preferable.
As in figure 2 it is shown, in this gas purge system, described heat exchanger 410 includes inner core 412 and the urceolus 411 being coaxially disposed,
Described inner core 412 is rotatable and urceolus 411 is fixed, and when inner core 412 rotates, will enter the raw material of reaction generating means 5
Material inlet 412J ' from inner core 412 enters inner core 412 cylinder and gradually flows to the raw material discharging opening on inner core 412
412C ', the slag charge then slag charge charging aperture 411J from urceolus 411 discharged from gas dust-removing device 6 enter urceolus 411 with interior
Cylinder 412 between and gradually flow to the slag charge discharging opening 411C on urceolus 411.Wherein, described material inlet 412J ' and slag
Material charging aperture 411J is respectively positioned on the same side of heat exchanger 410, described raw material discharging opening 412C ' and the equal position of slag charge discharging opening 411C
In the opposite side of heat exchanger 410, thus realize and flow heat exchange；Be respectively equipped with on the inner tube wall of described inner core 412 and outer tube wall with
The rotation of inner core 412 and promote what the material in inner core 412 and between inner core 412 and urceolus 411 moved to discharging direction to squeeze
Laminated structure.Extrusion structure is preferably selected spiral helicine rib or blade.And when flowing heat exchange, the rib inside and outside inner core 412 or blade
The hand of spiral should be consistent, but spiral angle can be the same or different.Exchange material inlet 412J ' and raw material discharging opening
The direction of 412C ' or the direction of exchange slag charge charging aperture 411J and slag charge discharging opening 411C will realize countercurrent flow.Adverse current is changed
During heat, rib or the hand of spiral of blade inside and outside inner core 412 should be contrary, but spiral angle can be the same or different.Adjust
The rotating speed of whole inner core 412 can change slag charge and the raw material time of staying in heat exchanger.
As it is shown in figure 1, when above-mentioned gas purge system is for oil shale retorting liquefaction, described reaction generating means 5 is dry
Evaporating reaction unit 1, described raw material is oil shale, and gas dust-removing device 6 i.e. dedusting system 2.At this moment, Ying Yousuo
State filtering residue in heat-exchange system 4, the oil shale that will enter dry distillation reactor device to be heated, to guarantee the oily page after this heating
Rock is from the dry distilling product that described dusty gas release end discharge outlet temperature is higher after entering dry distillation reactor device 1 reaction, and this goes out
Mouthful temperature guarantees to make dry distilling product still to reach >=the high temperature of 350 DEG C and ＜ 800 DEG C after gas dust-removing device 6 processes.Pass through heat exchange
The outlet of the dry distilling product that the oil shale after system 4 heating is discharged from dusty gas release end after entering dry distillation reactor device reaction
Temperature preferably can ensure that and makes this dry distilling product reach the >=high temperature of 450 DEG C and ＜ 800 DEG C after gas dust-removing device 6 processes.
As it is shown in figure 1, use above-mentioned gas purge system to realize, step that oil shale retorting method for producing oil includes is: one, from
The dry distilling product release end A of dry distillation reactor device 1 discharges dry distilling product and is passed through dedusting system 2；Two, through dedusting
System 2 processes the dry distilling product after obtaining slag charge and purifying, and described slag charge leads to heat-exchange system 4, and the dry distilling after described purification is produced
Thing leads to condensate recovery system 3；Three, described slag charge in heat-exchange system 4 to the oil shale that will enter dry distillation reactor device 1
Heat, discharge from dry distilling product release end A after entering dry distillation reactor device 1 reaction with the oil shale after guaranteeing this heating
The dry distilling product that outlet temperature is higher, this outlet temperature guarantees to make dry distilling product at condensate recovery system after dedusting system 2
The dry distilling product receiving terminal B of 3 still reaches >=350 DEG C (preferably 450 DEG C) and the inlet temperature of ＜ 800 DEG C；Four, by condensing back
Receipts system 3 condenses recovery step by step to the dry distilling product entered from described dry distilling product receiving terminal B.
When the dry distilling product receiving terminal B at condensate recovery system 3 reach >=inlet temperature of 350 DEG C and ＜ 800 DEG C time, described gas
In body dust pelletizing system 2, the filter element of the first gas purification units 210 should at its porous filter material tolerable 400 to 800 DEG C
Temperature range in filter；When dry distilling product receiving terminal B at condensate recovery system 3 reaches >=450 DEG C and ＜ 800 DEG C
During inlet temperature, in described dedusting system 2, the filter element of the first gas purification units 210 should be at its porous filter material
Filter in the temperature range of tolerable 500 to 800 DEG C.With porous filter material in the temperature range of 500 to 800 DEG C
As a example by work, it also is able to discharge the slag charge of high temperature (500 to 800 DEG C) from dedusting system.Even if by the heat exchange effect of 50%
Rate calculates, and the oil shale that will enter dry distillation reactor device the most also can be heated to about 250 DEG C, thus by oil shale
Surface water and combine water and be reduced to less than 2%.So, after the oil shale after being preheated enters dry distillation reactor device, it becomes possible to
Guarantee from the dry distilling product that dry distilling product release end discharge outlet temperature is higher.So circulation, oil shale retorting liquefaction system will reach
To and maintain a stable running status.
Embodiment 1
Oil shale retorting liquefaction system includes dry distillation reactor device 1 and condensate recovery system 3, and condensate recovery system 3 mainly includes
The three grades of condensation recovery bodys being made up of the air cooler 310 set gradually by condensation recovery route, water cooler 320, chiller 330
System, the bottom of every one-level cooler is equipped with shale oil discharge line；The dry distilling product release end A of described dry distillation reactor device 1
And being connected by dedusting system 2 between the dry distilling product receiving terminal B of condensate recovery system 3, this dedusting system 2 is wrapped
Include the first gas purification units 210 and to be arranged on the second gas of the first gas purification units 210 front end by udst separation direction clean
Changing unit 220, the second gas purification units 220 uses gravitational precipitator, and the first gas purification units 210 uses filtering accuracy
Be the intermetallic compound porous filtering material of FeAl of 5 microns be filter element；Dry distillation reactor device 1 and gas dust pelletizing system 2
Between be provided with heat-exchange system 4, this heat-exchange system 4 include through one heat exchanger 410 heat exchange connect first flow path 420 and second
Stream 430, described first flow path 420 is the oil shale loading channel of dry distillation reactor device 1, and second flow path 430 is removed for gas
The slag charge slagging channel of dirt system 2；This heat exchanger 410 includes inner core 412 and the urceolus 411 being coaxially disposed, and inner core 412 can
Rotate and urceolus 411 is fixed, when inner core 412 rotates, in oil shale oil shale charging aperture 412J from inner core 412 enters
Cylinder 412 cylinder and gradually flow to the oil shale discharging opening 412C on inner core 412, the slag charge then slag charge from urceolus 411 enters
Material mouth 411J enters between urceolus 411 and inner core 412 and gradually flows to the slag charge discharging opening 411C on urceolus 411, oil page
Rock charging aperture 412J and slag charge charging aperture 411J is respectively positioned on the same side of heat exchanger 410, and oil shale discharging opening 412C and slag charge go out
Material mouth 411C is respectively positioned on the opposite side of heat exchanger 410, and is respectively equipped with inner core 412 on the inner tube wall of inner core 412 and outer tube wall
Rotation and promote the helical blade that the object in inner core 412 and between inner core 412 and urceolus 413 moves to discharging direction.
The method realizing oil shale retorting liquefaction by this oil shale retorting liquefaction system is: after system stable operation, dry distillation reactor
The dry distilling product of the dry distilling product release end A discharge temperature about 600 DEG C of device 1, this dry distilling product is through the second gas purification units
220 rough dustings enter the first gas purification units 210 with the temperature of about 500 DEG C after purifying and filter, and the dry distilling after filtration is produced
In thing, dust content is reduced to 3mg/m3Hereinafter, subsequently into condensate recovery system 3；Dry distilling is produced by the air cooler 310 of the first order
The temperature of thing is down to about 450 DEG C, at this moment, obtains boiling point mink cell focus (not oil-containing more than 450 DEG C bottom air cooler 310
Mud, and solid content 3mg/m3Below)；The temperature of remaining dry distilling product is down to about 180 DEG C by the water cooler 320 of the second level,
At this moment, bottom air cooler 310, obtain the boiling point middle matter oil (not sludge containing, and solid content 3mg/m between 180 to 449 DEG C3
Below)；The temperature of remaining dry distilling product is down to about 40 DEG C by the chiller 330 of the third level, at this moment, from chiller 330
Bottom obtains boiling point light oil (not sludge containing, and solid content 3mg/m between 40 to 179 DEG C3Below)；Remaining dry distilling
Product is mainly shale gas；The slag charge about 500 DEG C discharged from the second gas purification units 220 and the first gas purification units 210
Left and right, carries out heat exchange with the oil shale that will enter dry distillation reactor device 1 after entering heat exchanger 410, makes oil shale be warming up to
300 DEG C, by the surface water of oil shale with combine water and be reduced to less than 2%, so that it is guaranteed that this oil shale is entering dry distillation reactor device
Make the thermograde in dry distillation reactor device 1 reduce during 1 reaction, reduce dry distilling heat absorption, thus dry distilling product release end A row
Go out the dry distilling product of outlet temperature about 600 DEG C.
The technique effect of this embodiment mainly has: 1) from 80%, the productivity of current oil shale is brought up to more than 99%, does not appoint
The waste of what shale oil；2) greasy filth is not produced, in traditional technique, it is impossible to the problem solving greasy filth can thoroughly solve；3)
Reduce production cost: by the improvement of this technique, the production cost of shale oil can be reduced by more than 15%, improve enterprise and exist
Competitiveness of the same trade, owing to technique shortens, its stability improves, and the expense of care and maintenance reduces the most accordingly；4) by oil
Dustiness in gas is disposably reduced to 3mg/m3Hereinafter, the problem in the subsequent production in technique is thoroughly solved；5) heavy is promoted
The yield of oil: in traditional technique, mink cell focus is easy to admixed together with greasy filth during cooling, it is impossible to separate, this
Secondary dedusting at high operating temperatures, mink cell focus is then easy to be refined out；6) make full use of heat energy, reduce the energy of whole process
Consumption；7) moisture of oil shale is reduced to less than 2%, reduces the heat absorption of retort process；3) thoroughly solve oil shale to heat not
Uniform phenomenon.
Claims (8)
1. can realize a gas purge system for slag heat utilization, including the reaction generating means (5) for producing dusty gas
And discharge the gas dust-removing device (6) that end is connected, this gas dust-removing device (6) with the dusty gas on this reaction generating means (5)
It is provided with slag-draining device, it is characterised in that: it is provided with heat exchange between described reaction generating means (5) and gas dust-removing device (6)
System (4), this heat-exchange system (4) includes the first flow path (420) through a heat exchanger (410) heat exchange connection and second
Road (430), described first flow path (420) is the raw materials passage of reaction generating means (5), and second flow path (430) is
The slag charge slagging channel of gas dust-removing device (6), this slagging channel is connected with described slag-draining device；Described heat exchanger (410)
Including the inner core (412) being coaxially disposed and urceolus (411), described inner core (412) is rotatable and urceolus (411) is fixed, when
When inner core (412) rotates, the raw material material inlet from inner core (412) (412J ') of reaction generating means (5) will be entered
Enter inner core (412) cylinder and gradually flow to raw material discharging opening on inner core (412) (412C '), from gas dust-removing device
(6) slag charge discharged the then slag charge charging aperture (411J) from urceolus (411) enters urceolus (411) and inner core (412)
Between and gradually flow to the slag charge discharging opening (411C) on urceolus (411), the inner tube wall of described inner core (412) and outer tube wall
On be respectively equipped with the rotation with inner core (412) and promote in inner core (412) and between inner core (412) and urceolus (411)
The extrusion structure that moves to discharging direction of material.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: described gas removes
Dirt device (6) at least includes the first gas purification units (210), and described first gas purification units (210) uses filters essence
Spending the porous filter material at 0.01 to 100 micron is filter element.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: described first gas
Body clean unit (210) employing filtering accuracy is filter element at the porous filter material of 0.1 to 10 micron.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: described porous mistake
Filtering material is the highest can be filtered at 800 DEG C.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: described gas removes
Dirt device (6) also includes the second gas purification list being arranged on the first gas purification units (210) front end by udst separation direction
Unit (220), described second gas purification units (220) uses one or both in mechanical dust collector and electrostatic precipitator.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: described raw material enters
Material mouth (412J ') and slag charge charging aperture (411J) are respectively positioned on the same side of heat exchanger (410), described raw material discharging opening (412C ')
With the opposite side that slag charge discharging opening (411C) is respectively positioned on heat exchanger (410).
A kind of gas purge system realizing slag heat utilization, it is characterised in that: when described gas
Body cleaning system is when oil shale retorting liquefaction, and described reaction generating means (5) is dry distillation reactor device (1), and described is former
Material is oil shale；Further, described slag charge in heat-exchange system (4), the oil shale that will enter dry distillation reactor device is added
Heat, discharges out from described dusty gas release end after entering dry distillation reactor device (1) reaction with the oil shale after guaranteeing this heating
The dry distilling product that mouthful temperature is higher, this outlet temperature guarantee to make dry distilling product still reach after gas dust-removing device (6) processes >=
The high temperature of 350 DEG C and ＜ 800 DEG C.
A kind of gas purge system realizing slag heat utilization, it is characterised in that: by heat exchange system
The outlet of the dry distilling product that the oil shale after system (4) heating is discharged from dusty gas release end after entering dry distillation reactor device reaction
Temperature can ensure that and makes this dry distilling product reach the >=high temperature of 450 DEG C and ＜ 800 DEG C after gas dust-removing device (6) processes.
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| CN103146405B (en) * | 2013-03-20 | 2017-02-08 | 李伟 | Oil shale dry distillation device and method |
| CN104109546B (en) * | 2013-04-18 | 2016-12-28 | 北京市工业设计研究院有限公司 | Multiple spot blanking upper-burning solid heat carrier retort technique |
| CN103816735B (en) * | 2014-02-28 | 2015-12-02 | 成都易态科技有限公司 | Gas filter system and device |
| CN104774627B (en) * | 2015-04-01 | 2018-01-30 | 曲靖众一精细化工股份有限公司 | A kind of block moving bed destructive distillation oil-gas recovery method and its retracting device |
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| CN101880540B (en) * | 2010-07-02 | 2013-06-19 | 西北化工研究院 | Low-coalification degree pulverized coal pyrolysis method and product prepared through the same |
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