CN1012684B - Process for dry distillation of oil shale - Google Patents
Process for dry distillation of oil shaleInfo
- Publication number
- CN1012684B CN1012684B CN 87102476 CN87102476A CN1012684B CN 1012684 B CN1012684 B CN 1012684B CN 87102476 CN87102476 CN 87102476 CN 87102476 A CN87102476 A CN 87102476A CN 1012684 B CN1012684 B CN 1012684B
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- China
- Prior art keywords
- oil shale
- district
- gas
- shale layer
- layer
- Prior art date
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- 239000004058 oil shale Substances 0.000 title claims abstract description 99
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims description 33
- 230000008569 process Effects 0.000 title description 25
- 239000007789 gas Substances 0.000 claims abstract description 137
- 238000010438 heat treatment Methods 0.000 claims abstract description 38
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 238000002485 combustion reaction Methods 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 230000006872 improvement Effects 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 16
- 229910052799 carbon Inorganic materials 0.000 abstract description 16
- 238000011084 recovery Methods 0.000 abstract description 10
- 239000002912 waste gas Substances 0.000 abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 25
- 150000002430 hydrocarbons Chemical class 0.000 description 15
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000010880 spent shale Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 206010011376 Crepitations Diseases 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 208000037656 Respiratory Sounds Diseases 0.000 description 1
- 230000005856 abnormality Effects 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
To keep the calorific value of produced gas constant irrespective of changes in the quality of oil shale and to enhance heat efficiency, by preheating an oil shale layer at a specified temp. before it is introduced into a dry distillation zone in dry-distilling oil shale by using a translation lattice device. At least part of an oil shale layer (a) is preheated with a hot gas stream (from a conduit 1) at 350-150 deg.C before the layer is introduced into a dry distillation zone II. Product gas obtd. by preheating oil shale in a cooling zone IV, heating it in an indirect heater 12, feeding it to a burner 21, mixing it with an oxygen-contg. gas 22 and burning part thereof is fed to a heat dry distillation zone II as hot gas. At least part of waste gas F of gas which has been used for the heating of gas in the heater 12 in the step B is used as the hot gas stream for preheating the oil shale layer in the step A. At least part of oxygen-contg. gas A preheated in a cooling zone V is used as gas 24 to be fed to a carbon recovery zone III and gas 22 to be fed to the burner 21.
Description
The present invention relates to the oil shale retort method, more clearly say the method that relates in following apparatus, carry out oil shale distillation, this device has the rotation fire grate, and be separately fixed at this rotation fire grate wind box up and down, the structure of wind box is that they keep airtight with the rotation fire grate, in case gas from corresponding wind box to external leakage (for convenience, below deserving to be called the equipment of stating) for rotating the fire grate retort.
When adopting the rotation fire grate retort dry rectificating oil shale of common name circular furnace grate or straight fire grate, basic operation is to make gas pass the solid block oil shale layer with meeting at right angles substantially, resinous shale is stated to transmit on the fire grate and with rotating fire grate and almost flatly moves jointly, heats like this or cooling oil shale.This operation to well-known in this kind equipment roasting with the cooling iron ore method similar.
The advantage of dry rectificating oil shale is in this rotation grate type retort, and resinous shale can grind into powder in treating processes, because as mentioned above, carrying out pyrogenous resinous shale is to be stated to rotate on the fire grate, and resinous shale itself moves with the form of fixed bed.
In the art as everybody knows resinous shale in retort process, can generate a lot of crackles, and become fragile.Thereby under minor impact, just be broken into powder.
If it is resinous shale to be added from the still top discharge at the bottom of the still when carrying out such equipment a kind of that oil shale retort is handled, then in still, form the moving-bed of resinous shale piece, when gas stream during through this moving-bed (this kind equipment is hereinafter referred to as " moving-bed equipment "), resinous shale piece bed collides and rubs owing to the resinous shale piece contacts each other in moving process, can produce a large amount of oil shale powder.
If it is very big to speak of the volume of the oil shale powder that produces above, gas stream just increases through the resistance of resinous shale piece bed, not only cause the power of air blast to increase, and gas stream also can form channel when resinous shale piece bed.Therefore resinous shale just can not reach abundant destructive distillation.In addition, a large amount of oil shale powder is sneaked in the empyreumatic oil of gained, and the quality of empyreumatic oil is significantly reduced.
For above-mentioned reasons, adopting and rotating grate type retort dry rectificating oil shale is a kind of good method, because it has the advantages that only generate very a spot of oil shale powder.
United States Patent (USP) 3325395,4058905 and 4082645 has proposed with the ordinary method of rotating grate type retort dry rectificating oil shale.Oil Shale Data Book at US Department of Commerce National Techical Lnformation Service, among the PB80-125636, also this class methods have been introduced with circular furnace grate retort process (hereinafter referred to as " conventional process ").
With reference to the system schematic of above-mentioned data volume, narrate the summary and the shortcoming thereof of conventional process below.
Fig. 2 is the system schematic of known a kind of direct heating process.Pass through partition wall a ' in proper order when being stated from the oil shale layer of rotating fire grate, heating dry distillation area W between the b ', carbon recovery zone X between partition wall b ' c, partition wall c, the first cooling zone Y and partition wall d between the d, during the second cooling zone Z between the e, contact with air-flow of delivering to each district respectively, resinous shale has promptly been finished operation stepss such as destructive distillation, recovery carbon and cooling.
In Fig. 2, the resinous shale piece is added in the rotation fire grate 1 on the heating dry distillation area W left side with resinous shale feeder (not shown) " on, formation oil shale layer 2 '.When rotating fire grate when moving, oil shale layer 2 ' at first enter heating dry distillation area W, the hot gas flow that contained destructive distillation is so incensed that in this district's resinous shale and combustion cycle gas contacts.Resinous shale is after the heating destructive distillation, and oil shale layer enters carbon recovery zone X.
Enter the oil shale layer 2 of carbon recovery zone X ' with air streams contact, make the organic carbon burning in the shale of still staying after the destructive distillation.Use by the thermogenetic hot gas of burning and make oil shale layer 2 ' bottom not be subjected to pyrogenous resinous shale as yet to finish destructive distillation.Oil shale layer 2 ' the enter first cooling zone Y then distinguishes it at this and contacts with circulating current and cooled off by it.After this oil shale layer 2 ' the enter second cooling zone Z, here it and air streams contact and by its further cooling.Oil shale layer 2 ' sensible heat reclaim after, oil shale layer 2 ' promptly by discharging in the system.
By heating dry distillation area W and carbon recovery zone X effluent air in company with distilled oil with distillate water and be introduced into gas-liquid separator S together, in separator, distilled oil and to distillate water separated from the gas.Gas is by gas blower 3 ' send.By discharging in the system, remaining gas is delivered to the first cooling zone Y as circulation gas to part gas as product gas.
Gas after the first cooling zone Y preheating, by gas blower 4 ' deliver to heating dry distillation area W, with after the preheating in the second cooling zone Z by the air mixed of gas blower 5 ' send here.Contained a part of distillate gas generation hot gas that therefore burns in the circulation gas.This hot gas is about to resinous shale heating destructive distillation.
Fig. 2 has also provided feed oil shale F, spent shale D, air A, burner B, compressor and water cooler PC, product gas PG and distilled oil and distillate water DOW.
As mentioned above, the advantage of process shown in Figure 2 is that air is directly sent into circulating current, makes a part of distillate gas burning, can easily obtain being used for the required hot gas of dry rectificating oil shale, and without any need for special equipment.But the shortcoming of following is that the product gas calorific value of gained is very low.
Fig. 3 illustrates a kind of known embodiment of indirect heating process.This example has improved the above-mentioned shortcoming of direct heating process.
In the process of Fig. 3, through the gas after the first cooling zone Y preheating indirect heater 6 ' in further heating, the hot gas of gained is sent among the heating dry distillation area W then.Adopt a part distillate gas as indirect heater 6 ' the energy.In the process of Fig. 3, the air that enters in the cycle gas system is only supplied with by the air of sending into carbon recovery zone X in order to reclaim carbon.Therefore compare with the product that Fig. 2 process obtains, the product of gained has the high advantage of calorific value.
In Fig. 2 and Fig. 3, the identical identical structure unit of reference symbol representative.WG represents combustion exhaust.In the process of Fig. 3, indirect heater 6 ' required heat transfer area becomes too big, so that is difficult to design a kind of dry distillation apparatus for oil shale of economy.If reduce heat transfer area with the temperature that improves indirect heater waste gas, then produced other shortcoming, promptly Zhuan Zhi thermo-efficiency reduces greatly.
The common drawback of Fig. 2 and Fig. 3 process is, when the content of water in the feed oil shale, oil shale retort can not fully realize, perhaps the oil shale retort device must be designed to unnecessary big throughput.
Be described in detail the reason of the problems referred to above below.
The inventor has measured the required heat of dry rectificating oil shale.According to the Fisher laboratory analysis of data, find consisting of of resinous shale:
Water-content: 9.24%(is heavy) (, being radix) with feed oil shale by the ratio of room temperature to the 500 ℃ whole water of destructive distillation gained
Hydrocarbon content: 8.94%(is heavy) (, being radix) with feed oil shale by the ratio of room temperature to the 500 ℃ whole hydrocarbon compounds of destructive distillation gained
Resistates content: 81.82%(is heavy)
According to the said determination result, be the 500 ℃ of above-mentioned resinous shale of destructive distillation institute heat requirements:
Required total heat: about 182 kilocalories of per kilogram feed oil shale
The analysis of required total heat:
The heat about 46% that destructive distillation water is required.
The heat about 0.5% that the destructive distillation hydro carbons is required.
Other (being mainly the sensible heat of resinous shale) about 53.5%.
Find out significantly that from the data of above mensuration the required heat major part of dry rectificating oil shale is consumed in and removes water, only seldom is consumed in the purposes of expection, promptly oil distillates.The big heat of this abnormality that destructive distillation water is required may be not only because evaporation of water latent heat is big, also owing to it is said that the heat of dissociation of the combination water that exists in the resinous shale is also big.
As everyone knows, not only the hydrocarbon content in the resinous shale changes greatly, and its water-content variation also very greatly, even the resinous shale of exploiting in the areal different location also is like this.In fact, the inventor has measured the sample of resinous shale, observes following variation (according to the assay method of Fisher).
Hydrocarbon content: 5.66-12.31%(is heavy) (is radix with feed oil shale)
Water content: 6.77-18.72%(is heavy) (is radix with feed oil shale)
The variation of water-content in this variation, particularly resinous shale means that the thermal load of dry distillation apparatus for oil shale alters a great deal.
In Fig. 2 and the described process of Fig. 3, the water content of resinous shale increases let us by the example imagination now.In order to finish the destructive distillation of institute's hydrocarbon-containifirst in the resinous shale, must improve the quantity that gas is sent in the gas temperature of sending into heating dry distillation area W or increase, to adapt to this variation.
If the gas temperature of sending into rises so high, the contained carbonate of resinous shale also begins to decompose, and the heat that is provided also is consumed in decomposing carbonate.This not only makes re-set target be difficult to realize, but also has produced other problem, promptly because the increase of gasification of hydrocarbons speed makes the quality of gained empyreumatic oil reduce the yield minimizing.
Everybody knows that also hydrocarbon content changes, and the productive rate of the inflammable gas component of destructive distillation gained (hydrogen, methane, ethane, propane etc.) also changes, and does not talk the yield variation of oil.The variation of these inflammable gas component productive rates can cause following difficulty.
In the common example of the direct heating process of Fig. 2, the distillate gas that heating dry distillation area W produces partly circulate and and air mixed, make a part of this circulation gas burning generate hot gas, this hot gas is used for the heating destructive distillation of resinous shale then.Much less, contained airborne rare gas element mainly is nitrogen and carbonic acid gas etc. in the combustion exhaust, also mixes with the circulation gas phase, thereby has reduced the calorific value of circulation gas.
When the inflammable gas components contents of destructive distillation generation changed, when descending, the calorific value of circulation gas obviously reduced, and may be difficult to continue to keep burning especially.In order to overcome this difficult problem, need a kind ofly can make combustion stablized measure, for example, as auxiliary thermal source, and adjust heat with a part of distilled oil that burns.But this measure is unworthy recommending, and also can reduce because do the yield that can not effectively utilize distillate gas while oil like this.
In the device of the distillate gas that is used for obtaining high heating value, as the process among Fig. 3, the variation of distillate gas quantity can not cause trouble.But another problem has appearred, and promptly must be the sizable degree of the indirect heater 6 used ' be amplified to the feeding gas heating that does not enter heating dry distillation area W as yet.
A kind of potential danger of the indirect heater 6 that the gas of being made up of hydrocarbon compound is used ' comprise, promptly because the decomposition of hydrocarbon compound, the tube wall of well heater may carbon deposit.Consider this potential danger, the gas temperature of heating usefulness can not rise very highly.The heat transfer coefficient of gas-gas heat exchange is very little again.In addition, speak of above, the required heat that dewaters from resinous shale is very big.Consider these situations, familiar technician recognizes easily, must install a uneconomic big indirect heater as indirect heater 6 ', be used for taking off main impurity-water.
Everybody is also clear, and except the water-content variation of resinous shale, the yield of the inflammable gas component that dry rectificating oil shale generates also alters a great deal.In the known embodiment of the direct heating process of routine, distillate gas circulates, and oxygen-containing gas then is admitted in a part of circulation distillate gas, makes its burning and obtains destructive distillation hot gas, its shortcoming is there is not suitable stable operational condition, changes because the front has been spoken of the calorific value of circulation gas.
Obtain the distillate gas of high heating value in order to overcome above-mentioned shortcoming, proposed the known embodiment of above-mentioned conventional heat-processed, promptly obtain destructive distillation gas with indirect heater.But be used for from capital cost, this terms of settlement is unworthy recommending, because toply talk about, indirect heater must be done very greatly.
It is irrelevant that a target of the present invention provides a kind of variation with feed oil shale quality, can keep product gas calorific value constant retort process.More particularly, the intent of the present invention is (1) even when the water-content of feed oil shale changes, and does not also need to change the operational condition of rotating the fire grate retort and can finish oil shale retort; (2) even when the hydrocarbon content of resinous shale descends, also can make the inflammable gas burning of destructive distillation gained, thereby the hot gas that stably provides destructive distillation to use; (3) improve the thermo-efficiency of dry distillation apparatus for oil shale; (4) use low-quality heat,, produce the distillate gas of high heating value as the used heat that burning is worked off one's feeling vent one's spleen; (5) realize purpose (1) with the dry distillation apparatus for oil shale of necessary minimum size, (2), (3) and (4) in other words, provide a kind of oil shale retort device of economy.
As mentioned above, in the required total heat of dry rectificating oil shale, about 50% heat is used for the contained water of dry rectificating oil shale.The inventor distinguishes that most of water contained in the resinous shale can be removed having carried out a large amount of experimental studies aspect the oil shale retort characteristic when contacting with air-flow.The temperature of air-flow should be lower than the actual temperature that begins to decompose of hydrocarbon compound in the resinous shale, but is higher than 150 ℃ (recommending 350-200 ℃).
That is to say that it is owing to notice the following fact that the inventor obtains the present invention, promptly the required required total heat of heat as many as dry rectificating oil shale of destructive distillation water is about 50%, can be in advance with the gas of lesser temps the water destructive distillation be fallen.
One aspect of the present invention provide a kind of in the rotation grate type retort in first district and second district and/or the 3rd district is set the process of dry rectificating oil shale.This process comprises following sequential steps; (ⅰ) resinous shale of chunky shape is carried through first district, in this district, be stated from the oil shale layer of the chunky shape on the rotation fire grate, contact with the hot gas flow of the oil shale layer of flowing through and resinous shale is heated destructive distillation; (ⅱ) oil shale layer of carrying gained is through second district, and in this district, oil shale layer contacts with the oxysome that contains of the oil shale layer of flowing through; And/or the oil shale layer of carrying gained is through the 3rd district, and in this district, oil shale layer is cooled off by the air-flow of the oil shale layer of flowing through.In addition, (a) oil shale layer enters before first district, and at least a portion oil shale layer and temperature are that 350-150 ℃ hot gas flow contacts, thereby are preheated; (b) hot gas that feeds first district is a gas after the first-class combustion that obtains with the mixing of another part oxygen-containing gas of giving vent to anger of being discharged by a burning part first district in the burner, and this is first-class gives vent to anger and be preheated in the 3rd district and by a further preheating of indirect heater; (c) at least a portion is heated first-class second effluent gases of giving vent to anger and obtaining by the indirect heater in (b), as the hot gas flow of at least a portion oil shale layer in the preheating (a); (d) oxygen-containing gas of the oil shale layer in the 3rd district that flows through that at least a portion is other and preheating therein is as supplying with the oxygenous of second district, the another kind of oxygenous burner of then delivering in (b).
According to process of the present invention, most of oil removes from resinous shale, resinous shale enter first district promptly heat dry distillation area before preheating.Therefore even when the water-content of feed oil shale changes, can in rotation fire grate retort, under steady operation conditions, finish oil shale retort.
Feed oil shale contacts with air-flow in the preheating zone.The dust that cracks in incidental dust of resinous shale or the resinous shale and generate can be removed along with air-flow.Therefore avoided dust to sneak in the product oil that promptly heats dry distillation area and generated in first district.This quality to oil produces a kind of good influence.
Since dual-purpose direct heating and two kinds of technology of indirect heating, when destructive distillation feed oil shale, even when the quality change of feed oil shale caused the inflammable gas change of production, the calorific value of circulation gas can remain unchanged, thereby can keep the constant combustion conditions.
Because direct heating burner and indirect heater are combined, therefore can reduce the thermal load of indirect heater.Like this, compare with conventional indirect heater, just can dwindle the size of indirect heater, the result helps to reduce capital cost.As mentioned above, because utilized the lower effluent gases of temperature of discharging to do the hot gas that preheating is used, so pyrogenous overall thermal efficiency height by indirect heater.
By following specification sheets of the present invention, additional claims and relevant accompanying drawing can clearly be seen that above-mentioned purpose of the present invention and other purpose, its characteristic and advantage.
Fig. 1 is the system schematic of an embodiment of expression process of the present invention;
Fig. 2 is illustrated in the system schematic of rotating a kind of conventional process of dry rectificating oil shale in the fire grate retort;
Fig. 3 is illustrated in the system schematic of rotating the another kind of conventional process of dry rectificating oil shale in the fire grate retort.
With reference now to Fig. 1.One deck feed oil shale bed (hereinafter referred to as " oil shale layer ") a is stated from and transmits on the fire grate sequentially by a preheating zone (district's I), the combustion flow that resinous shale is sent here by pipeline 1 in this district preheating of giving vent to anger; A heating dry distillation area (district's II), the hot gas heating destructive distillation sent here by pipeline 2 of the resinous shale of preheating in this district; A carbon recovery zone (district's III), remaining organic carbon contacts with oxygen-containing gas that pipeline 3 is sent here and burns in the resinous shale in this district after the destructive distillation; One first cooling zone (district's IV), the cold air cooling that oil shale layer is sent here by pipeline 4 in this district; One second cooling zone (district's V), the air A that oil shale layer is sent here by pipeline 5 in this district further cools off.Then, resinous shale is discharged in system as spent shale b.
The effluent of district's I is sent to gas-liquid separator 6, and the water in the effluent promptly is removed, and discharges in system as water PW.And the gas in the effluent as waste gas PG by gas blower 7 through pipeline 8 discharge systems.If desired, the effluent of district's II can cool off in water cooler 9.Then this effluent is delivered to gas-liquid separator 10.In gas-liquid separator 10, fall by the dried simultaneously distilled of district's II oil and water are separated, remaining gas is delivered to by gas blower 11 and is used to distinguish the indirect heater 12 of IV and is used for burner 13 to carbon recovery zone supply hot gas.Any remaining gas is then discharged system through pipeline 14 as product gas PG.
Isolated oil and water are sent to oil-water separator 15 in gas-liquid separator 10.Product oil PO discharges in system through pipeline 16, and water is discharged through pipeline 17.The gas of delivering to district's IV by pipeline 4 with heat and carry out heat exchange by the oil shale layer that has wherein reclaimed organic carbon, gas just is preheated like this.The gas of preheating through pipeline 19 draw and with mix mutually from the cold air of pipeline 18.The mixed gas of gained is delivered to indirect heater 12 heating by gas blower 20.
After indirect heater 12 heating, gas is delivered to destructive distillation burner 21, this with send here by pipeline 22 in second cooling zone air of preheating mix mutually.Part gas promptly burns the hot gas of using for destructive distillation.This destructive distillation hot gas is sent into district's II.
The preferred temperature scope that enters district's II gas is 450 °-800 ℃ (500-700 ℃ more suitable), and in order to guarantee this temperature range, the thermal load of burner 21 and indirect heater 12 can be adjusted according to the variation of feed oil shale quality.Below narrate this specific program.For example, when the turnout of inflammable gas in heating dry distillation area (district's II) reduces, the calorific value thereby the reduction of district's II effluent gases, the thermal load that at this moment can increase indirect heater 12 remains unchanged the calorific value of circulation gas and product gas PG.
After pipeline 23 is delivered to the gas combustion that burner 13 is used for the carbon recovery zone with deliver to burner 13 through pipeline 24 and mix mutually in the excess air of second cooling zone preheating.Part gaseous combustion and the temperature of gas is raise.Deliver to district's III through the gas after heating like this.In district's III, still stay the organic carbon burning in the resinous shale.The burning gas of heat flows out district's III.This gas is delivered to indirect heater 12 as thermal source.
A part is also delivered to indirect heater 12 through pipeline 26 by the effluent gases of district's II through the circulation gas that the solution-air separation obtains.This part circulation gas with send into through pipeline 25 oxygenously mix afterfire, promptly obtain heating the hot gas of usefulness.The hot gas and the heated gas of the heating usefulness that obtains like this carry out heat exchange, then as waste gas FG through pipeline 27 discharge systems.Part waste gas is sent into district's I through pipeline 1.
The gas temperature of sending into district's I is high more good more, but this temperature should be lower than the actual temperature that begins to decompose of hydrocarbon compound in the resinous shale.If temperature surpasses the decomposition temperature of hydrocarbon compound, then gaseous hydrocarbon compound will be sneaked into through pipeline 8 and be discharged in the gas of system.On the other hand, if temperature is on the low side, the effect of resinous shale preheating is with regard to variation.
Except the effluent gases of indirect heater 12, also the gas that heated can be sent into district's I through gas blower 28 in district's V.If desired, after also a part of product gas can being burnt in the burner (not shown), the combustion exhaust with gained merges application again.
As mentioned above, the process of Fig. 1 is applicable to the resinous shale that water-content and hydrocarbon content alter a great deal.This is a kind ofly to keep product gas calorific value constant simultaneously, retort process that can quiet run.Should be pointed out that and the hot gas that a kind of preheating is used can be sent into the hopper (not shown) of feed oil shale, rather than send into district's I preheating, feed oil shale after the preheating, just can be handled in rotating the fire grate retort in hopper.According to the present invention, can make loading hopper increase preheating and functions/drying, and loading hopper now have only as a kind of function of raw materials bucket.Therefore can dwindle the size of rotating the fire grate retort, a kind of dry distillation apparatus for oil shale of economy promptly is provided.Industrial effect of the present invention thereby be significant.
The present invention now all narrates and finishes, and clearly, a those of ordinary skill in the art can make many changes and improvement to this under the situation that does not break away from the present invention's spirit and scope described herein.
Claims (1)
1, the method for dry rectificating oil shale in a rotation fire grate retort that first district and second district and/or the 3rd district be set, this method comprises the step of following order:
(i) resinous shale of carrying chunky shape, is stated from the chunky shape oil shale layer of rotating on the fire grate and contacts with the hot gas flow that passes oil shale layer in this district through first district, thereby makes resinous shale heating destructive distillation; With
The oil shale layer of (ii) carrying gained is through second district, and in this district, oil shale layer contacts with the oxygen flow of the oil shale layer of flowing through; And/or the oil shale layer of carrying gained is through the 3rd district, and in this district, oil shale layer is cooled off by the air-flow of the oil shale layer of flowing through, and its improvements are:
(a) oil shale layer enters before first district, and at least a portion oil shale layer and temperature are that 350-150 ℃ hot gas flow contacts, thereby are preheated;
(b) hot gas that feeds first district is a gas after the first-class combustion that obtains with the mixing of another part oxygen-containing gas of giving vent to anger of being discharged by a burning part first district in the burner, and this is first-class gives vent to anger and be preheated in the 3rd district and by a further preheating of indirect heater;
(c) with at least a portion by first-class second effluent gases that obtains the hot gas flow of giving vent to anger of the indirect heater in (b) heating as at least a portion oil shale layer in the preheating (a); With
(d) the other oxygenous oxygen-containing gas of at least a portion once being flowed through oil shale layer and in the 3rd district, being preheated in the 3rd district as supply second district, the another kind of oxygenous burner of then supplying with in (b).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP285906/86 | 1986-12-02 | ||
| JP28590686A JPS63139980A (en) | 1986-12-02 | 1986-12-02 | Method of dry-distilling oil shale |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN87102476A CN87102476A (en) | 1988-06-22 |
| CN1012684B true CN1012684B (en) | 1991-05-29 |
Family
ID=17697548
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87102476 Expired CN1012684B (en) | 1986-12-02 | 1987-04-02 | Process for dry distillation of oil shale |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPS63139980A (en) |
| CN (1) | CN1012684B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101402870B (en) * | 2008-11-20 | 2010-05-12 | 沈阳成大弘晟能源研究院有限公司 | Complete alternation gas retort for treating 300 tons of wax shale mash gas a day |
| CN102220148B (en) * | 2010-04-19 | 2014-03-26 | 山东省冶金设计院股份有限公司 | Heating method at oil shale temperature rise section in rotary grate type retort |
| CN103087740B (en) * | 2013-01-22 | 2014-12-10 | 中国重型机械研究院股份公司 | Small-size oil shale dry distillation system heated based on heat accumulation type gas radiation pipe |
| CN107133683B (en) * | 2016-02-26 | 2021-06-15 | 中国石油化工股份有限公司 | Probability prediction method for thermal fracture of oil shale |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57207682A (en) * | 1981-06-15 | 1982-12-20 | Mitsubishi Heavy Ind Ltd | Dry distillation of oil shale |
| JPS587482A (en) * | 1981-07-07 | 1983-01-17 | Mitsubishi Heavy Ind Ltd | Carbonizing method of oil shale |
-
1986
- 1986-12-02 JP JP28590686A patent/JPS63139980A/en active Pending
-
1987
- 1987-04-02 CN CN 87102476 patent/CN1012684B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN87102476A (en) | 1988-06-22 |
| JPS63139980A (en) | 1988-06-11 |
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