CN102876343A - System for making oil by retorting oil shale - Google Patents
System for making oil by retorting oil shale Download PDFInfo
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- CN102876343A CN102876343A CN2012103155062A CN201210315506A CN102876343A CN 102876343 A CN102876343 A CN 102876343A CN 2012103155062 A CN2012103155062 A CN 2012103155062A CN 201210315506 A CN201210315506 A CN 201210315506A CN 102876343 A CN102876343 A CN 102876343A
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Abstract
The invention discloses a system for making oil by retorting oil shale. By the system, the yield of oil sludge can be reduced. The system comprises a retorting reaction device, a condensation recovery system, wherein the retorting product releasing end of the retorting reaction device is connected with the retorting product receiving end of the condensation recovery system through a gas dedusting system; the gas dedusting system at least comprises a first gas purification unit; and the first gas purification unit takes a porous filtering material of which the filtering precision is 0.01 to 80 micrometers as a filtering element. The retorting product is purified by the porous filtering material of which the filtering precision is 0.01 to 80 micrometers before condensation, so that the dust content of the retorting product can be greatly reduced, and the yield of the subsequent oil sludge is reduced. The system is particularly suitable to serve as a system for making the oil by using a retorting gas heat carrier in an internal heating mode.
Description
Technical field
The present invention relates to resinous shale destructive distillation (upground retorting) on the ground technology, be specifically related to oil shale distillation liquefaction system.
Background technology
Oil shale distillation is divided into underground retoring (underground retorting) and (the upground retorting) two kinds of destructive distillation on the ground.Wherein, though the underground retoring technology is applied for a patent by Shell Co. Ltd, but still be in development, there is no industrial applications.Destructive distillation on the ground is still the main path of resinous shale development and use.Resinous shale destructive distillation on the ground is divided into again two kinds of external-heat destructive distillation and internal heat type destructive distillation.The external-heat destructive distillation refers to that thermal barrier carries out destructive distillation by the furnace wall resinous shale of heating in stove, and this technology is eliminated at present; The internal heat type destructive distillation refers to that thermal barrier directly contacts with resinous shale, carries out destructive distillation in stove, be the mainstream technology of present resinous shale development and use.The thermal barrier of internal heat type destructive distillation is divided into gaseous heat-carrier and solid thermal carriers.In general, no matter be gaseous heat-carrier internal heat type destructive distillation liquefaction system, or solid thermal carriers internal heat type destructive distillation liquefaction system, all comprise dry distillation reactor device and condensate recovery system.The application is defined as the dry distillation reactor device resinous shale is carried out destructive distillation hot-work and produces destructive distillation product and the outside device that discharges this destructive distillation product, condensate recovery system is defined as the system that the destructive distillation product is carried out condensation and reclaims.
For gaseous heat-carrier internal heat type destructive distillation liquefaction system, the destructive distillation product that discharges from the dry distillation reactor device directly enters condensate recovery system.Wherein, there are Chinese Fushun formula system, Brazilian Pei Teluosekesi (Petrosix) system, Estonia's Abel Kiviat (Kiviter) system etc. in most typical gaseous heat-carrier internal heat type destructive distillation liquefaction system.For solid thermal carriers internal heat type destructive distillation liquefaction system, because the material that discharges from the dry distillation reactor device is by the shale ashes of making solid thermal carriers, the shale semicockes and the destructive distillation product that generate mix, to pass through gravitational precipitator at present, the dust removal with machine equipment such as cyclonic separator separate the destructive distillation product of gaseous state with shale ashes and the shale semicockes of solid, then the destructive distillation product is imported condensate recovery system, the shale ashes of telling and the mixture of shale semicockes then burn, its temperature is reached about 800 ℃, more again as the solid thermal carriers of dry rectificating oil shale.Wherein, there is Ta Seke (Taciuk) system (also claiming ATP) of Estonian Ge Luote (Galoter) system, Australia etc. in most typical solid thermal carriers internal heat type destructive distillation liquefaction system.
In a word, no matter gaseous heat-carrier internal heat type destructive distillation liquefaction system or solid thermal carriers internal heat type destructive distillation liquefaction system, when the destructive distillation product enters condensate recovery system all with a certain amount of dust.For gaseous heat-carrier internal heat type destructive distillation liquefaction system, Source of Dust mainly is the solid matter of being taken out of the dry distillation reactor device with air-flow; For solid thermal carriers internal heat type destructive distillation liquefaction system, Source of Dust mainly is the solid matter that is not got off by the dust removal with machine device separates.In the gaseous heat-carrier internal heat type destructive distillation liquefaction system, when the destructive distillation product enters condensate recovery system with dust more, can generate relatively large greasy filth.The greasy filth amount of gaseous heat-carrier internal heat type destructive distillation liquefaction system is less comparatively speaking.Greasy filth is the mixture of water, shale oil and dust.Shale oil accounts for about 30% in the greasy filth that gaseous heat-carrier internal heat type destructive distillation liquefaction system generates, and dust accounts for about 20%.If greasy filth can not get timely processing, not only cause the oil loss, and impact is produced.The main path that reduces at present greasy filth be strengthen entering the screening of the resinous shale of dry distillation reactor device, improve resinous shale distribution, improve that air-flow in the dry distillation reactor device distributes and heat supply ratio and the temperature out that reduces the dry distillation reactor device.Wherein, the temperature out purpose that reduces the dry distillation reactor device is to make the top of dry distillation reactor device form the warm and humid bed of material, thereby reduces the discharge of dust.
As seen, prior art has been instructed undoubtedly by the temperature out that reduces the dry distillation reactor device and has been reduced the greasy filth generation.An interesting phenomenon correspondingly is, in the present gaseous heat-carrier internal heat type destructive distillation liquefaction system, the temperature out of dry distillation reactor device is generally lower, and the temperature out of dry distillation reactor device is that 80 to 100 ℃, the temperature out of Brazilian Pei Teluosekesi (Petrosix) system are about 150 ℃ in the formula system of Chinese Fushun as previously mentioned.Shale oil can be divided into mink cell focus, middle matter oil and lightweight oil usually.The division of mink cell focus, middle matter oil and lightweight oil is not strict.The application is defined as mink cell focus with boiling point in the part more than 450 ℃, and the part of boiling point between 180 to 449 ℃ is defined as middle matter oil, and just the part of boiling point between 40 to 179 ℃ is defined as lightweight oil.Because at present the temperature out of dry distillation reactor device is lower in the gaseous heat-carrier internal heat type destructive distillation liquefaction system, the shale oil that therefore is recovered to from condensate recovery system be mink cell focus, matter oil and lightweight oil mixture.This just makes troubles for the later use of shale oil.There is such problem equally in solid thermal carriers internal heat type destructive distillation liquefaction system.
Summary of the invention
＜first part 〉
First technical problem that the application is intended to solve provides a kind of oil shale distillation liquefaction system that reduces greasy filth output.
For this reason, the application's oil shale distillation liquefaction system comprises dry distillation reactor device and condensate recovery system, the destructive distillation product of described dry distillation reactor device discharges between the destructive distillation product receiving end of end and condensate recovery system and links to each other by the dedusting system, this dedusting system comprises the first gas purification units at least, and described the first gas purification units employing filtering accuracy is filtering element at 0.01 to 80 micron porous filter material.Thereby porous filter material filters the purpose except mainly reaching by the solids in the material interception gas itself, in filtration procedure, less solids also can form at material surface and put up a bridge, thereby set up less cavity to increase the interception result to solids.In addition, porous filter material also has the mode that gravity settling, inertial impaction etc. capture solid particulate concurrently, has further improved filter effect.Therefore, after the porous filter material of condensation front employing filtering accuracy in above-mentioned interval range implemented to purify to the destructive distillation product, the dust content in the destructive distillation product can greatly reduce, thereby obviously reduces the output 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 adopts filtering accuracy when the porous filter material below 10 microns is filtering element, owing to higher filtering accuracy, the dust content in the destructive distillation product after the processing of dedusting system can be reduced to 5mg/m at least
3Below.At this moment, the product that condensation obtains is essentially the liquid substance that mainly is comprised of shale oil and water, does not have the greasy filth composition.This provides condition for the technical process of simplifying condensate recovery system, also can improve the productive rate of shale oil simultaneously.Can guarantee higher filtration efficiency and the filtering accuracy of porous filter material is controlled at more than 0.1 micron.Based on such reason, it is filtering element at 0.1 to 10 micron porous filter material that the first gas purification units among the application preferably adopts filtering accuracy.
In the larger situation of Dust Capacity that the dedusting system need process, for fear of to the frequent pulse cleaning of the first gas purification units, described dedusting system also comprises the second gas purification units that is arranged on the first gas purification units front end by the udst separation direction, and described the second gas purification units adopts one or both in mechanical dust collector and the electrostatic precipitator.The second gas purification units can be carried out to the destructive distillation product that just enters the dedusting system one-level or what purifying treatment, remove the most dust in the destructive distillation product, the Dust Capacity that enters in the first gas purification units will greatly be reduced, thereby improve the time of the first gas purification units continuous firing, reduce the blowback frequency.
The slag charge waste heat that gets off in order to utilize the dedusting system to capture, be provided with heat-exchange system between described dry distillation reactor device and the gas dust-removal system, this heat-exchange system comprises the first stream and the second stream that connects through exchanger heat exchange, the resinous shale that described the first stream is the dry distillation reactor device passage that feeds in raw material, the second stream is the slag charge slagging channel of dedusting system.For existing gaseous heat-carrier internal heat type destructive distillation liquefaction system, owing to not being provided for capturing the equipment of dust in the destructive distillation product between dry distillation reactor device and the condensate recovery system, also just can not utilize the dust heat that captures that the resinous shale that is about to enter the dry distillation reactor device is carried out preheating.For existing solid thermal carriers internal heat type destructive distillation liquefaction system, what trap is the mixture of shale ashes and shale semicockes, therefore after must burning, this mixture as solid thermal carriers, also is difficult to directly the resinous shale that is about to enter the dry distillation reactor device be carried out preheating with this mixture.In a word, the above-mentioned this UTILIZATION OF VESIDUAL HEAT IN mode of the application is skillfully constructed, and can the waste heat that the dedusting system captures the slag charge that gets off effectively be utilized.
Mention in the application's background technology because the temperature out of dry distillation reactor device is lower, the shale oil that is recovered to from condensate recovery system be mink cell focus, matter oil and lightweight oil mixture, thereby make troubles for the utilization of shale oil.To this, the temperature out that (mainly being in the temperature range that porous filter material can tolerate in the first gas purification units) improves the dry distillation reactor device as much as possible in the scope that the dedusting system can bear becomes the direction that the application considers.And above-mentioned slag charge UTILIZATION OF VESIDUAL HEAT IN mode is exactly the important channel that the application improves dry distillation reactor device temperature out.The application's concrete scheme is: described destructive distillation product discharges the temperature out of end and guarantees to make the filtering element in the first gas purification units to filter in 400 to 800 ℃ the temperature range that its porous filter material can tolerate; And, described condensate recovery system have to the temperature in that enters from described destructive distillation product receiving end 〉=350 ℃ and＜800 ℃ destructive distillation product carries out the system that step by step condensation is reclaimed.This scheme will guarantee that in fact exactly porous filter material works in 400 to 800 ℃ temperature range, make the temperature in energy of destructive distillation product receiving end 〉=350 ℃ and＜800 ℃, in order in follow-up condensation removal process, mink cell focus, middle matter oil are separated with lightweight oil.
Just in time because porous filter material is worked, therefore also can discharge the slag charge of high temperature from the dedusting system in 400 to 800 ℃ temperature range.Even the heat exchange efficiency by 50% calculates, the resinous shale that is about to enter the dry distillation reactor device at least also can be heated to about 200 ℃, thereby is reduced to about 2% with the surface water of resinous shale with in conjunction with water.Like this, after the resinous shale after being preheated enters the dry distillation reactor device, just can guarantee that discharging end from the destructive distillation product discharges the higher destructive distillation product of temperature out.So circulation, oil shale distillation liquefaction system will reach and maintain a stable running status.
Certainly, the filtering element in described the first gas purification units preferably can filter in 500 to 800 ℃ temperature range; And the temperature in of described destructive distillation product receiving end 〉=450 ℃ and＜800 ℃.Like this, can also from shale oil, tell at least the middle matter oil of a part.
The application's oil shale distillation liquefaction system also further provides a kind of heat exchange efficiency higher interchanger.Specifically, this interchanger comprises inner core and the urceolus of coaxial setting, described inner core is rotatable and urceolus is fixed, when inner core rotates, resinous shale enters the cylindrical shell of inner core and flows to gradually resinous shale discharge port on the inner core from the resinous shale opening for feed on the inner core, and the slag charge then slag charge opening for feed from the urceolus enters between urceolus and the inner core and flows to gradually slag charge discharge port on the urceolus.Urceolus can effectively prevent the heat of slag charge to the outside diffusion of interchanger, and the inner core of rotation can make resinous shale wherein be heated evenly, and the length of urceolus and inner core can guarantee enough heat-exchange times.Therefore, this interchanger can be realized the high efficient heat exchanging between solid and the solid.Recently say mutually, this exchanger heat conductance is higher, and the heat-transfer effect of whole process is better.
Wherein, described resinous shale opening for feed and slag charge opening for feed preferably are positioned at the same side of interchanger, and described resinous shale discharge port and slag charge discharge port then are positioned at the opposite side of interchanger, to form and the stream heat exchange.In addition, preferably also be respectively equipped with on the inner tube wall of described inner core and the wall of the outer-rotor rotation with inner core promote in the inner core and inner core and urceolus between object to the extrusion structure of discharging direction motion, such as spiral helicine rib, blade etc.Like this, as long as can change resinous shale and the residence time of slag charge in interchanger by the rotating speed of adjusting inner core, in order to improve heat transfer effect according to concrete needs.Certainly, if above-mentioned extrusion structure is not set fully or the extrusion structure that is positioned on the inner core inner tube wall only is set, also can be with inner core and urceolus integral body to discharging direction inclination certain angle (preferably being set as 10 to 30 °), in order to rely on gravity that material is flowed voluntarily.
In sum, the application's oil shale distillation liquefaction system can reduce even eliminate the greasy filth that produces in the condensation removal process on the one hand, thereby the temperature out that can improve on the one hand the dry distillation reactor device under energy saving condition makes shale oil be segmented recovery, have marked improvement than prior art, especially be suitable as gaseous heat-carrier internal heat type destructive distillation liquefaction system.
＜second section 〉
Second technical problem that the application is intended to solve provides a kind of oil shale distillation method of making oil that makes shale oil be segmented recovery.The following content of this " second section " can be understood with reference to the content of " first part ".
For this reason, the step that comprises of the application's oil shale distillation method of making oil is: one, discharge end from the destructive distillation product of dry distillation reactor device and discharge the destructive distillation product and pass into the dedusting system; Two, the destructive distillation product after the processing of dedusting system obtains slag charge and purifies, described slag charge leads to heat-exchange system, and the destructive distillation product after the described purification leads to condensate recovery system; Three, described slag charge heats the resinous shale that is about to enter the dry distillation reactor device in heat-exchange system, guaranteeing that resinous shale after this heating discharges end from the destructive distillation product and discharges the higher destructive distillation product of temperature out after entering the dry distillation reactor device reaction, this temperature out guarantee to make destructive distillation product destructive distillation product receiving end at condensate recovery system after the dedusting system still reach 〉=350 ℃ and＜800 ℃ temperature in; Four, by condensate recovery system the destructive distillation product that enters from described destructive distillation product receiving end being carried out step by step condensation reclaims.
Just as what mention in above-mentioned " first part ", the method brings up to the temperature in of destructive distillation product receiving end under energy saving condition 〉=350 ℃ and＜800 ℃, that is to say, compared with prior art, the application has improved the temperature of destructive distillation product when beginning to carry out the condensation recovery more than 200 ℃ fully, therefore, in follow-up step by step condensation removal process, just can access the shale oil of relative segmentation.Based on alleged cause in above-mentioned " first part ", the temperature out that after entering the dry distillation reactor device reaction, discharges the destructive distillation product that end discharges from the destructive distillation product by the resinous shale after the heat-exchange system heating can guarantee to make this destructive distillation product destructive distillation product receiving end at condensate recovery system after the dedusting system processes reach 〉=450 ℃ and＜800 ℃ temperature in.
For the application's oil shale distillation method of making oil, the method that dedusting system and nonessential use are filtered.This be because, in the application's the oil shale distillation method of making oil, the primary effect of dedusting system is to capture dust, therefore, even if adopt traditional dust removal with machine device (for example gravitational precipitator or tornado dust collector) also can realize such purpose.Certainly, the application advises that still described dedusting system comprises the first gas purification units at least, it is filtering element at 0.01 to 80 micron porous filter material that described the first gas purification units adopts filtering accuracy, and this filtering element can be at 400(that its porous filter material can tolerate preferably 500) to 800 ℃ temperature range, filter.
Based on alleged cause in above-mentioned " first part ", in the larger situation of Dust Capacity that the dedusting system need process, described dedusting system preferably also comprises the second gas purification units that is arranged on the first gas purification units front end by the udst separation direction, and described the second gas purification units adopts one or both in mechanical dust collector and the electrostatic precipitator.Can improve like this time of the first gas purification units continuous firing, reduce the blowback frequency.
Equally based on alleged cause in above-mentioned " first part ", it is filtering element at 0.1 to 10 micron porous filter material that described the first gas purification units adopts filtering accuracy, so that the dust content in will the destructive distillation product after the dedusting system processes is reduced to 5mg/m
3Below.
Concrete structure as heat-exchange system, described heat-exchange system comprises the first stream and the second stream that connects through exchanger heat exchange, the resinous shale that described the first stream is the dry distillation reactor device passage that feeds in raw material, the second stream is the slag charge slagging channel of dedusting system.
Wherein, described interchanger comprises inner core and the urceolus of coaxial setting, described inner core is rotatable and urceolus is fixed, when inner core rotates, resinous shale enters the inner core cylindrical shell and flows to gradually resinous shale discharge port on the inner core from the resinous shale opening for feed on the inner core, and the slag charge then slag charge opening for feed from the urceolus enters between urceolus and the inner core and flows to gradually slag charge discharge port on the urceolus.
Further be, described resinous shale opening for feed and slag charge opening for feed all are positioned at the same side of interchanger, and described resinous shale discharge port and slag charge discharge port all are positioned at the opposite side of interchanger.
Further be, be respectively equipped with on the inner tube wall of described inner core and the wall of the outer-rotor rotation with inner core promote in the inner core and inner core and urceolus between object to the extrusion structure of discharging direction motion.
＜third part 〉
The 3rd technical problem that the application is intended to solve provides a kind of gas treating system that realizes the slag thermal utilization.The following content of this " third part " can be understood with reference to the content of " second section ".
To this, this gas treating system comprise for generation of dusty gas the reaction generating unit with this reaction generating unit on dusty gas discharge the gas dust-removing device that end links to each other, this gas dust-removing device is provided with slag discharging device, be provided with heat-exchange system between described reaction generating unit and the gas dust-removing device, this heat-exchange system comprises the first stream and the second stream that connects through exchanger heat exchange, described the first stream is the raw materials passage of reaction generating unit, the second stream is the slag charge slagging channel of gas dust-removing device, and this slagging channel links to each other with described slag discharging device.
Further be, described gas dust-removing device comprises the first gas purification units at least, and described the first gas purification units employing filtering accuracy is filtering element at 0.01 to 100 micron porous filter material.
Further be that described the first gas purification units employing filtering accuracy is filtering element at 0.1 to 10 micron porous filter material.
Wherein, described porous filter material is the highest can filter under 800 ℃.
Further be, described gas dust-removing device also comprises the second gas purification units that is arranged on the first gas purification units front end by the udst separation direction, and described the second gas purification units adopts one or both in mechanical dust collector and the electrostatic precipitator.
Further be, described interchanger comprises inner core and the urceolus of coaxial setting, described inner core is rotatable and urceolus is fixed, when inner core rotates, the raw material that is about to enter the reaction generating unit enters the inner core cylindrical shell and flows to gradually raw material discharge port on the inner core from the material inlet on the inner core, and the slag charge of discharging from the gas dust-removing device then slag charge opening for feed from the urceolus enters between urceolus and the inner core and flows to gradually slag charge discharge port on the urceolus.
Further be, described material inlet and slag charge opening for feed all are positioned at the same side of interchanger, and described raw material discharge port and slag charge discharge port all are positioned at the opposite side of interchanger.
Further be, be respectively equipped with on the inner tube wall of described inner core and the wall of the outer-rotor rotation with inner core promote in the inner core and inner core and urceolus between material to the extrusion structure of discharging direction motion.
When described gas treating system was used for the oil shale distillation liquefaction, described reaction generating unit was the dry distillation reactor device, and described raw material is resinous shale; And, the resinous shale that is about to enter the dry distillation reactor device is heated in heat-exchange system by described filter residue, guaranteeing that resinous shale after this heating discharges end from described dusty gas and discharges the higher destructive distillation product of temperature out after entering the dry distillation reactor device reaction, this temperature out guarantee to make the destructive distillation product after gas dust-removing device is processed, still reach 〉=350 ℃ and＜800 ℃ high temperature.
Further be, the temperature out that after entering the dry distillation reactor device reaction, discharges the destructive distillation product that end discharges from dusty gas by the resinous shale after the heat-exchange system heating can guarantee to make this destructive distillation product after gas dust-removing device is processed, reach 〉=450 ℃ and＜800 ℃ high temperature.
The present invention is described further below in conjunction with the drawings and specific embodiments.The aspect that the application adds and advantage in the following description part provide, and part will become obviously from the following description, or recognize by the application's practice.
Description of drawings
Fig. 1 is the principle schematic (process flow sheet) of the application's oil shale distillation liquefaction system.
Fig. 2 is the structural representation of interchanger in the application's oil shale distillation liquefaction system.
Embodiment
At first by reference to the accompanying drawings a kind of gas treating system of slag thermal utilization that realizes of the application is specifically described.
As shown in Figure 1, this gas treating system comprises, for generation of dusty gas reaction generating unit 5 with this reaction generating unit 5 on dusty gas discharge the gas dust-removing device 6 that end links to each other, this gas dust-removing device 6 is provided with slag discharging device, be provided with heat-exchange system 4 between described reaction generating unit 5 and the gas dust-removing device 6, this heat-exchange system 4 comprises the first stream 420 and the second stream 430 that connects through an interchanger 410 heat exchanges, described the first stream 420 is the raw materials passage of reaction generating unit 5, the second stream 430 is the slag charge slagging channel of gas dust-removing device 6, and this slagging channel links to each other with described slag discharging device.Existing gas gas dust-removing device 6 cleaning apparatuss 6 generally have with slag discharging device.Such as, the bottom of gas dust-removing device 6 is the design of back taper normally, and oral area is useful on the valve of discharging.Some slag discharging devices also may adopt the machinery of more complicated, and commonly used have a spiral discharging machine etc.Gas dust-removing device 6 can only adopt one or more in existing gravitational precipitator, tornado dust collector and the electrostatic precipitator.Said " the first stream 420 " and " the second stream 430 " general reference raw materials route and slag charge deslagging route generally include one or more in transport pipe, the conveying belt in the reality." heat exchange connection " refers to that the first stream 420 and the second stream 430 can directly realize the physics heat exchange.The key of this gas treating system is that the slag charge preheating of the enough gas dust-removing devices 6 of energy will enter the raw material of this reaction generating unit 5, save energy.
As shown in Figure 1, in this gas treating system, described gas dust-removing device 6 comprises the first gas purification units 210 at least, and described the first gas purification units 210 employing filtering accuracies are filtering element at 0.01 to 100 micron porous filter material.In order to guarantee higher filtering accuracy and higher filtration efficiency, it is filtering element at 0.1 to 10 micron porous filter material that the first gas purification units 210 preferably adopts filtering accuracy.In addition, if gas dust-removing device 6 will at high temperature be worked, selected porous filter material should the highlyest can filter under 800 ℃.Satisfy such condition, selectable porous filter material is mainly sintering metal porous material or ceramic porous material.Preferred FeAl intermetallic compound porous material, TiAl intermetallic compound porous material or NiAl intermetallic compound porous material in the sintering metal porous material, this class material has higher high-temperature corrosion-resistance, filtering accuracy and workability, has good Integrated using performance.On this basis, gas dust-removing device 6 also comprises the second gas purification units 220 that is arranged on the first gas purification units 210 front ends by the udst separation direction, and described the second gas purification units 220 adopts one or both in mechanical dust collector and the electrostatic precipitator.The first gas purification units 210 and the collocation of the second gas purification units 220 result of use of getting up is better.
As shown in Figure 2, in this gas treating system, described interchanger 410 comprises inner core 412 and the urceolus 411 of coaxial setting, described inner core 412 is rotatable and urceolus 411 is fixing, when inner core 412 rotates, the raw material that is about to enter reaction generating unit 5 enters inner core 412 cylindrical shells and flows to gradually raw material discharge port 412C ' on the inner core 412 from the material inlet 412J ' on the inner core 412, and the slag charge of discharging from the gas dust-removing device 6 then slag charge opening for feed 411J from the urceolus 411 enters the slag charge discharge port 411C that also flows to gradually between urceolus 411 and the inner core 412 on the urceolus 411.Wherein, described material inlet 412J ' and slag charge opening for feed 411J all are positioned at the same side of interchanger 410, and described raw material discharge port 412C ' and slag charge discharge port 411C all are positioned at the opposite side of interchanger 410, thereby realize and the stream heat exchange; Be respectively equipped with on the inner tube wall of described inner core 412 and the wall of the outer-rotor rotation with inner core 412 promote in the inner core 412 and inner core 412 and urceolus 411 between material to the extrusion structure of discharging direction motion.Extrusion structure is preferably selected spiral helicine rib or blade.And stream is during heat exchange, and the rib that inner core 412 is inside and outside or the hand of spiral of blade should be consistent, but spiral angle can be the same or different.Transposing material inlet 412J ' will realize countercurrent flow with the direction of raw material discharge port 412C ' or the direction of transposing slag charge opening for feed 411J and slag charge discharge port 411C.During countercurrent flow, the rib inside and outside the inner core 412 or the hand of spiral of blade should be opposite, but spiral angle can be the same or different.The rotating speed of adjusting inner core 412 can change slag charge and the residence time of raw material in interchanger.
As shown in Figure 1, when above-mentioned gas treating system was used for the oil shale distillation liquefaction, described reaction generating unit 5 was dry distillation reactor device 1, and described raw material is resinous shale, and gas dust-removing device 6 is dedusting system 2.At this moment, should in heat-exchange system 4, be heated the resinous shale that is about to enter the dry distillation reactor device by described filter residue, guaranteeing that resinous shale after this heating discharges end from described dusty gas and discharges the higher destructive distillation product of temperature out after entering 1 reaction of dry distillation reactor device, this temperature out guarantee to make the destructive distillation product after gas dust-removing device 6 is processed, still reach 〉=350 ℃ and＜800 ℃ high temperature.The temperature out that after entering the dry distillation reactor device reaction, discharges the destructive distillation product that end discharges from dusty gas by the resinous shale after heat-exchange system 4 heating preferably can guarantee to make this destructive distillation product after gas dust-removing device 6 is processed, reach 〉=450 ℃ and＜800 ℃ high temperature.
As shown in Figure 1, the step of using above-mentioned gas treating system to realize that the oil shale distillation method of making oil comprises is: one, the destructive distillation product from dry distillation reactor device 1 discharges end A discharge destructive distillation product and passes into dedusting system 2; Two, the destructive distillation product after 2 processing of dedusting system obtain slag charge and purify, described slag charge leads to heat-exchange system 4, and the destructive distillation product after the described purification leads to condensate recovery system 3; Three, described slag charge heats the resinous shale that is about to enter dry distillation reactor device 1 in heat-exchange system 4, guaranteeing that resinous shale after this heating discharges end A from the destructive distillation product and discharges the higher destructive distillation product of temperature out after entering 1 reaction of dry distillation reactor device, this temperature out guarantee to make destructive distillation product destructive distillation product receiving end B at condensate recovery system 3 after dedusting system 2 still reach 〉=350 ℃ (preferred 450 ℃) and＜800 ℃ temperature in; Four, carrying out step by step condensation by 3 pairs of destructive distillation products that enter from described destructive distillation product receiving end B of condensate recovery system reclaims.
When the destructive distillation product receiving end B at condensate recovery system 3 reach 〉=350 ℃ and＜during 800 ℃ temperature in, the filtering element of the first gas purification units 210 should filter in 400 to 800 ℃ the temperature range that its porous filter material can tolerate in the described dedusting system 2; When the destructive distillation product receiving end B at condensate recovery system 3 reach 〉=450 ℃ and＜during 800 ℃ temperature in, the filtering element of the first gas purification units 210 should filter in 500 to 800 ℃ the temperature range that its porous filter material can tolerate in the described dedusting system 2.Work as example in 500 to 800 ℃ temperature range take porous filter material, also can discharge the slag charge of high temperature (500 to 800 ℃) from the dedusting system.Even the heat exchange efficiency by 50% calculates, the resinous shale that is about to enter the dry distillation reactor device at least also can be heated to about 250 ℃, thereby is reduced to below 2% with the surface water of resinous shale with in conjunction with water.Like this, after the resinous shale after being preheated enters the dry distillation reactor device, just can guarantee that discharging end from the destructive distillation product discharges the higher destructive distillation product of temperature out.So circulation, oil shale distillation liquefaction system will reach and maintain a stable running status.
Embodiment 1
Oil shale distillation liquefaction system comprises dry distillation reactor device 1 and condensate recovery system 3, condensate recovery system 3 mainly comprises three grades of condensation recovery system that are comprised of the air cooler 310, water cooler 320, the deep freezer 330 that set gradually by condensation recovery route, and the bottom of every one-level water cooler is equipped with the shale oil escape route; The destructive distillation product of described dry distillation reactor device 1 discharges between the destructive distillation product receiving end B of end A and condensate recovery system 3 and links to each other by dedusting system 2, this dedusting system 2 comprises the first gas purification units 210 and is arranged on the second gas purification units 220 of the first gas purification units 210 front ends by the udst separation direction, the second gas purification units 220 adopts gravitational precipitator, and the first gas purification units 210 employing filtering accuracies are that 5 microns the intermetallic compound porous filtering material of FeAl is filtering element; Be provided with heat-exchange system 4 between dry distillation reactor device 1 and the gas dust-removal system 2, this heat-exchange system 4 comprises the first stream 420 and the second stream 430 that connects through an interchanger 410 heat exchanges, the resinous shale that described the first stream 420 is dry distillation reactor device 1 passage that feeds in raw material, the second stream 430 is the slag charge slagging channel of dedusting system 2; This interchanger 410 comprises inner core 412 and the urceolus 411 of coaxial setting, inner core 412 is rotatable and urceolus 411 is fixing, when inner core 412 rotates, resinous shale enters the cylindrical shell of inner core 412 and flows to gradually resinous shale discharge port 412C on the inner core 412 from the resinous shale opening for feed 412J on the inner core 412, the slag charge then slag charge opening for feed 411J from the urceolus 411 enters between urceolus 411 and the inner core 412 and flows to gradually slag charge discharge port 411C on the urceolus 411, resinous shale opening for feed 412J and slag charge opening for feed 411J all are positioned at the same side of interchanger 410, resinous shale discharge port 412C and slag charge discharge port 411C all are positioned at the opposite side of interchanger 410, and be respectively equipped with on the inner tube wall of inner core 412 and the wall of the outer-rotor rotation with inner core 412 promote in the inner core 412 and inner core 412 and urceolus 413 between object to the screw-blade of discharging direction motion.
The method that realizes the oil shale distillation liquefaction by this oil shale distillation liquefaction system is: behind the system stable operation, the destructive distillation product of dry distillation reactor device 1 discharges approximately 600 ℃ destructive distillation product of end A outflow temperature, this destructive distillation product enters the first gas purification units 210 with about 500 ℃ temperature and filters after the second gas purification units 220 rough dustings purify, dust content is reduced to 3mg/m in the destructive distillation product after the filtration
3Below, then enter condensate recovery system 3; The air cooler 310 of the first step is down to the temperature of destructive distillation product about 450 ℃, at this moment, obtains boiling point at (not sludge containing, and the solid content 3mg/m of the mink cell focus more than 450 ℃ from air cooler 310 bottoms
3Below); The water cooler 320 of the second stage is down to the temperature of remaining destructive distillation product about 180 ℃, at this moment, from air cooler 310 bottoms obtain boiling point between 180 to 449 ℃ matter oil (not sludge containing, and solid content 3mg/m
3Below); The deep freezer 330 of the third stage is down to the temperature of remaining destructive distillation product about 40 ℃, at this moment, obtains lightweight oil (not sludge containing, and the solid content 3mg/m of boiling point between 40 to 179 ℃ from deep freezer 330 bottoms
3Below); Remaining destructive distillation product is mainly shale gas; The slag charge of discharging from the second gas purification units 220 and the first gas purification units 210 is approximately about 500 ℃, enter behind the interchanger 410 with the resinous shale that is about to enter dry distillation reactor device 1 and carry out heat exchange, make resinous shale be warming up to 300 ℃, be reduced to below 2% with the surface water of resinous shale with in conjunction with water, thereby guarantee that this resinous shale reduces the thermograde in the dry distillation reactor device 1 when entering 1 reaction of dry distillation reactor device, reduce the destructive distillation heat absorption, discharge approximately 600 ℃ destructive distillation product of temperature out thereby discharge end A at the destructive distillation product.
The technique effect of this embodiment mainly contains: 1) productive rate of present resinous shale is brought up to more than 99% from 80%, without any the waste of shale oil; 2) do not produce greasy filth, in traditional technique, the problem that can't solve greasy filth can thoroughly solve; 3) reduce production costs: by the improvement of this technique, the production cost of shale oil can be reduced more than 15%, improve enterprise in the competitive power of the same industry, because technique shortens, its stability improves, and the expense of care and maintenance also reduces accordingly; 4) with the disposable 3mg/m that is reduced to of the dustiness in the oil gas
3Below, thoroughly solve the problem in the subsequent production in the technique; 5) output of lifting mink cell focus: in traditional technique, mink cell focus is easy to greasy filth admixed together in the process of cooling, can't separate, and this dedusting under the condition of high temperature, mink cell focus then is easy to be refined out; 6) take full advantage of heat energy, reduced the energy consumption of whole process; 7) moisture with resinous shale is reduced to below 2%, reduces the heat absorption of retort process; 3) thoroughly solve the inhomogeneous phenomenon of resinous shale heating.
Claims (10)
1. oil shale distillation liquefaction system, comprise dry distillation reactor device (1) and condensate recovery system (3), it is characterized in that: the destructive distillation product of described dry distillation reactor device (1) discharges between the destructive distillation product receiving end (B) of end (A) and condensate recovery system (3) and links to each other by dedusting system (2), this dedusting system (2) comprises the first gas purification units (210) at least, and described the first gas purification units (210) employing filtering accuracy is filtering element at 0.01 to 80 micron porous filter material.
2. oil shale distillation liquefaction as claimed in claim 1 system is characterized in that: it is filtering element at 0.1 to 10 micron porous filter material that described the first gas purification units (210) adopts filtering accuracy.
3. oil shale distillation liquefaction as claimed in claim 1 system, it is characterized in that: described dedusting system (2) also comprises the second gas purification units (220) that is arranged on the first gas purification units (210) front end by the udst separation direction, and described the second gas purification units (220) adopts one or both in mechanical dust collector and the electrostatic precipitator.
4. such as claim 1,2 or 3 described oil shale distillation liquefaction systems, it is characterized in that: be provided with heat-exchange system (4) between described dry distillation reactor device (1) and the gas dust-removal system (2), this heat-exchange system (4) comprises the first stream (420) and the second stream (430) that connects through an interchanger (410) heat exchange, described the first stream (420) is the reinforced passage of the resinous shale of dry distillation reactor device (1), and the second stream (430) is the slag charge slagging channel of dedusting system (2).
5. oil shale distillation liquefaction as claimed in claim 4 system, it is characterized in that: described destructive distillation product discharges the temperature out of end (A) and guarantees to make the filtering element in the first gas purification units (210) to filter in 400 to 800 ℃ the temperature range that its porous filter material can tolerate; And, described condensate recovery system (3) have to the temperature in that enters from described destructive distillation product receiving end (B) 〉=350 ℃ and＜800 ℃ destructive distillation product carries out the system that step by step condensation is reclaimed.
6. oil shale distillation liquefaction as claimed in claim 5 system, it is characterized in that: the filtering element in described the first gas purification units (210) can filter in 500 to 800 ℃ temperature range; The temperature in of described destructive distillation product receiving end (B) 〉=450 ℃ and＜800 ℃.
7. oil shale distillation liquefaction as claimed in claim 4 system, it is characterized in that: described interchanger (410) comprises inner core (412) and the urceolus (411) of coaxial setting, described inner core (412) is rotatable and urceolus (411) fixing, when inner core (412) rotates, resinous shale enters the cylindrical shell of inner core (412) and flows to gradually resinous shale discharge port (412C) on the inner core (412) from the resinous shale opening for feed (412J) on the inner core (412), and the slag charge then slag charge opening for feed (411J) from the urceolus (411) enters the slag charge discharge port (411C) that also flows to gradually between urceolus (411) and the inner core (412) on the urceolus (411).
8. oil shale distillation liquefaction as claimed in claim 7 system, it is characterized in that: described resinous shale opening for feed (412J) and slag charge opening for feed (411J) all are positioned at the same side of interchanger (410), and described resinous shale discharge port (412C) and slag charge discharge port (411C) all are positioned at the opposite side of interchanger (410).
9. oil shale distillation liquefaction as claimed in claim 7 system is characterized in that: be respectively equipped with on the inner tube wall of described inner core (412) and the wall of the outer-rotor rotation with inner core (412) promote in the inner core (412) and inner core (412) and urceolus (413) between object to the extrusion structure of discharging direction motion.
10. oil shale distillation liquefaction as claimed in claim 1 system is characterized in that: described oil shale distillation liquefaction system is gaseous heat-carrier internal heat type destructive distillation liquefaction system.
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| CN117431083A (en) * | 2023-11-15 | 2024-01-23 | 中石化胜利油建工程有限公司 | Shale oil dry distillation oil extraction device and process |
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