CN103131447B - Destructive distillation method and device for fluidized bed of oil shale - Google Patents
Destructive distillation method and device for fluidized bed of oil shale Download PDFInfo
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- CN103131447B CN103131447B CN201110413811.0A CN201110413811A CN103131447B CN 103131447 B CN103131447 B CN 103131447B CN 201110413811 A CN201110413811 A CN 201110413811A CN 103131447 B CN103131447 B CN 103131447B
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Abstract
The invention discloses a destructive distillation method and a device for a fluidized bed of oil shale to solve the problems that charking loading born by a charking appliance is enabled to be high, charking temperature is hard to control, and the charking appliance is prone to be damaged by over temperature due to the fact that one charking appliance is utilized to conduct charking in the prior art. The destructive distillation method includes the following steps: A. mixing a oil shale raw materials (90) with a high-temperature carrier in a bed type charking appliance (1), enabling the mixed oil shale materials and the high-temperature carrier to enter a bed type destructive distillation reactor (26) to conduct a destructive distillation reaction, stripping carried oil gas in the formed mixed semi-coke through stream, and enabling the mixed semi-choke to enter into a pipe type charking appliance (25); B. conducting one-stage charking on the mixed semi-choke which enters the pipe type charking appliance along the pipe type charking appliance; C. enabling the mixed semi-choke which is conducted the one-stage charking to enter the bed type charking appliance (1) to conduct two-stage charking. The invention discloses the destructive distillation device used for achieving the destructive distillation method for the fluidized bed of the oil shale. The destructive distillation method and the device for the fluidized bed of the oil shale are mainly used for destructive distillation processing of various granularity oil shale raw materials.
Description
Technical field
The invention belongs to oil shale distillation technical field, relate to a kind of fluidized bed dry distillation method and apparatus of resinous shale.
Background technology
Along with the scarcity day by day of petroleum resources and the arrival of Waste Era of Oil, countries in the world utilize oil shale distillation technology to produce shale oil, have become important aspect alternative, that supplement petroleum resources.Resinous shale is called again oil shale, is a kind of organic sedimentogeneous rock that contains.Organism in resinous shale consists of two kinds of materials conventionally: a kind of is bituminous matter, and another kind of is high molecular polymer (being referred to as oil female).Inorganics in resinous shale mainly contains quartz, kaolin, clay, mica, carbonatite and sulfurous iron ore etc.Resinous shale, after heating destructive distillation, generates shale oil, carbonization gas and shale semicockes.Shale oil can, directly as oil fuel, also can further produce the vehicle fuels such as gasoline, diesel oil.The fluidized bed dry distillation technology of resinous shale, there is the features such as destructive distillation hot strength is high, dry distillation rate fast, the shale oil quality better of generation, oil-collecting ratio height, referring to the introduction of the documents such as Chinese patent CN101440293A, < < Coal Chemical Industry > > magazine the 3rd phase of June in 2009 " resinous shale solid thermal carriers fluidized retoring oil refining process pilot scale research " (document 1).
Technique described in CN101440293A and document 1, some discharges destructive distillation device the generated high-temperature heat carrier of making charcoal in the device of making charcoal (cycling hot ash or high temperature shale ashes) after heat-obtaining, and separately some mixes, is heated with resinous shale raw material; After dry distillation reactor, generate the mixing semicoke that shale semicockes and thermal barrier mix, mix semicoke burning-off coke in the device of making charcoal and generate high-temperature heat carrier.Use high-temperature heat carrier as oil shale distillation thermal source, energy consumption is lower.The composition of high-temperature heat carrier of the present invention, the high temperature shale ashes that the device of making charcoal described in the cycling hot ash that the device (being circulating fluidized bed combustor) that is equivalent to make charcoal described in CN101440293A generates or document 1 generates.Above-mentioned retorting technique, all that a large amount of high heating value mixing semicokes that generate after dry distillation reactor are all sent into the device of making charcoal make charcoal (being burning-off coke), the load of making charcoal that the device that makes to make charcoal is born is higher, causes that charcoal temperature is difficult to control, the easy overtemperature of the device of making charcoal damages.
Summary of the invention
The fluidized bed dry distillation method and apparatus that the object of this invention is to provide a kind of resinous shale, with solve existing oil shale fluidized bed dry distillation technology existing because of use the device of making charcoal to make charcoal to make make charcoal the load of making charcoal that device bears higher, cause charcoal temperature to be difficult to the problem of controlling and the easy overtemperature of the device of making charcoal damages.
For addressing the above problem, the technical solution used in the present invention is: a kind of fluidized bed dry distillation method of resinous shale, is characterized in that: the method in turn includes the following steps:
A. the resinous shale raw material after pulverizing enters mixing tube through resinous shale material feeding tube, the high-temperature heat carrier that bed formula is made charcoal in device enters mixing tube through high-temperature heat carrier transfer lime, outlet by mixing tube after resinous shale raw material and high-temperature heat carrier mix in mixing tube enters bed formula dry distillation reactor device, resinous shale raw material carries out dry distillation reactor in bed formula dry distillation reactor device dense bed, generate shale oil, carbonization gas and shale semicockes, shale semicockes and thermal barrier in bed formula dry distillation reactor device dense bed are mixed to form mixing semicoke mutually, the cyclonic separator of the oil gas that dry distillation reactor generates in being located at bed formula dry distillation reactor device isolated and mixed half and defocusedly by bed formula dry distillation reactor device, flowed out, mixing semicoke in bed formula dry distillation reactor device dense bed flows downward, enter the stripping stage of being located at bed formula dry distillation reactor device below, in stripping stage, pass into water stripping steam, stripping goes out to mix semicoke entrained oil gas, mixing semicoke in stripping stage after stripping flows to the bottom of stripping stage, through semicoke transfer lime, enter the make charcoal bottom of device of tubular type,
B. enter the mixing semicoke that tubular type makes charcoal in device and contact with one section of air of making charcoal, along tubular type, making charcoal, device is up to carry out one section and makes charcoal;
C. one section of mixing semicoke after making charcoal enters the bed formula device of making charcoal by the make charcoal outlet of device of tubular type, in bed formula is made charcoal device dense bed, contact with two sections of air of making charcoal and carry out two sections and make charcoal, remaining coke on burning-off mixing semicoke, generate high-temperature heat carrier, make charcoal and two sections of flue gases of generating of making charcoal are discharged by the bed formula device of making charcoal after the cyclonic separator of being located at bed formula and making charcoal in device is isolated high-temperature heat carrier for one section, the high-temperature heat carrier that bed formula is made charcoal in device dense bed is flowed out by the bed formula device of making charcoal, a part is discharged destructive distillation device after heat-obtaining cooling, another part enters in mixing tube through high-temperature heat carrier transfer lime, mix with resinous shale raw material.
For realizing the fluidized bed dry distillation device of the resinous shale of aforesaid method, comprise a bed formula dry distillation reactor device, the bed formula device of making charcoal, the mixing device that also has resinous shale raw material and high-temperature heat carrier, and with bed formula the make charcoal heat-obtaining discharger of high-temperature heat carrier in device dense bed of bed formula that device is connected of making charcoal, it is characterized in that: the fluidized bed dry distillation device of resinous shale is also provided with the tubular type device of making charcoal, bed formula dry distillation reactor device is located at the make charcoal below of device of bed formula, in bed formula dry distillation reactor device, be provided with cyclonic separator, the top of bed formula dry distillation reactor device is provided with oil gas collection chamber and oil gas vent pipe, below is provided with stripping stage, in stripping stage, be provided with stripping baffles, stripped vapor sparger, the bottom of stripping stage is provided with semicoke transfer lime, which is provided with semicoke flowrate control valve, the make charcoal bottom of device of the outlet of semicoke transfer lime and tubular type is connected, the make charcoal bottom of device of tubular type is provided with one section of air-distributor of making charcoal, the make charcoal outlet of device of tubular type passes into bed formula and makes charcoal in device, bed formula is made charcoal in device and is provided with cyclonic separator, the make charcoal top of device of bed formula is provided with flue gas collection chamber and smoke outlet tube, bottom is provided with two sections of air-distributors of making charcoal, the mixing device of described resinous shale raw material and high-temperature heat carrier is mixing tube, the outlet of mixing tube passes in bed formula dry distillation reactor device, the entrance of mixing tube is connected with the outlet of high-temperature heat carrier transfer lime with the outlet of resinous shale material feeding tube, the entrance of high-temperature heat carrier transfer lime passes into bed formula and makes charcoal in device, the described bed formula heat-obtaining discharger of high-temperature heat carrier in device dense bed of making charcoal comprises high-temperature heat carrier drainage conduit, the entrance of high-temperature heat carrier drainage conduit and the bed formula device of making charcoal is connected, outlet is connected with heat collector, heat collector is connected with thermal barrier blow-down drum by pipeline, in high-temperature heat carrier transfer lime and high-temperature heat carrier drainage conduit, be equipped with high-temperature heat carrier flowrate control valve.
Adopt the present invention, there is following beneficial effect: (1) the present invention adopts tubular type device and the bed formula two sections of compound technology of making charcoal of device of making charcoal of making charcoal, and each device of making charcoal is only born a part for the load of always making charcoal, all lower.Like this, just make the charcoal temperature of two devices of making charcoal all easily control, the device overtemperature that prevented from making charcoal damages, and can guarantee the device long-term operation of making charcoal.And, tubular type make charcoal device and bed formula make charcoal the scantlings of the structure of device can be less.(2) two sections of compound technology of making charcoal of the present invention, the ability of making charcoal is strong, mix semicoke and make charcoal completely (mixing semicoke is made charcoal in device after two sections are made charcoal in make charcoal device and bed formula of tubular type, conventionally can more than 95% coke of burning-off), thereby can recycle more coke heat output.(3) the present invention has used the tubular type device of making charcoal; Compare with the conventional bed formula device of making charcoal, the tubular type utensil of making charcoal has the stronger ability of making charcoal and better turndown ratio.In tubular type, make charcoal in device, mix semicoke and contact with fresh air all the time, make to make charcoal speed and the efficiency of making charcoal are higher; Thus, also can reduce the make charcoal reserve of high-temperature heat carrier in device of bed formula, dwindle the make charcoal scantlings of the structure of device of bed formula, reduce investment outlay.
The present invention is mainly used in the destructive distillation processing of various granular resinous shale raw materials.
Below in conjunction with accompanying drawing, embodiment and embodiment, the present invention is further detailed explanation.Accompanying drawing, embodiment and embodiment do not limit the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the fluidized bed dry distillation device of resinous shale of the present invention.
Embodiment
Referring to Fig. 1, the fluidized bed dry distillation device (referred to as destructive distillation device) of resinous shale of the present invention, comprise a bed formula dry distillation reactor device 26, the bed formula device 1 of making charcoal, the mixing device that also has resinous shale raw material and high-temperature heat carrier, and with bed formula the make charcoal heat-obtaining discharger of device dense bed 20 interior high-temperature heat carriers of bed formula that device 1 is connected of making charcoal.Destructive distillation device is also provided with the tubular type device 25 of making charcoal.
Bed formula dry distillation reactor device 26 is located at the make charcoal below of device 1 of bed formula.The housing of bed formula dry distillation reactor device 26 is mainly comprised of superposed cylindrical metal cylindrical shell and the inverted round table face shape metal cylinder that is positioned at bottom, liner insulating and wearing-resistant lining (figure slightly).In bed formula dry distillation reactor device 26, be provided with cyclonic separator; Cyclonic separator shown in Fig. 1, for the dipleg of the first cyclonic separator 12 of being installed in series and 13, two cyclonic separators of the second cyclonic separator stretches in bed formula dry distillation reactor device dense bed 27 (stretching to the top of bed formula dry distillation reactor device dense bed 27).The top of bed formula dry distillation reactor device 26 is provided with oil gas collection chamber 24 and oil gas vent pipe 31, and below is provided with stripping stage 14; The top of stripping stage 14 is connected with the bottom of bed formula dry distillation reactor device 26.The housing of stripping stage 14 is mainly comprised of a cylindrical metal cylindrical shell, liner insulating and wearing-resistant lining (figure slightly).In stripping stage 14, be provided with stripping baffles (shown in Fig. 1 is herring-bone stripping baffles), stripped vapor sparger 7.The overall structure of the formula of bed shown in Fig. 1 dry distillation reactor device 26-stripping stage 14, similar to fluid catalytic cracking (FCC) settling vessel in petroleum refining process.The bottom of stripping stage 14 is provided with semicoke transfer lime 15, which is provided with semicoke flowrate control valve 30, to mix the flow of semicoke in control tube.Semicoke transfer lime 15 shown in Fig. 1, its entrance is connected in the bottom of stripping stage 14; The entrance of semicoke transfer lime 15 also can be connected in the bottom (figure slightly) of stripping stage 14 sides.
The make charcoal bottom of device 25 of the outlet of semicoke transfer lime 15 and tubular type is connected, and the make charcoal bottom of device 25 of tubular type is provided with one section of air-distributor 28 of making charcoal.The make charcoal outlet of device 25 of tubular type passes into bed formula and makes charcoal in device 1, is to be generally positioned at the make charcoal top at device dense bed 20 interfaces of bed formula.The make charcoal overall structure of device 25 of tubular type shown in Fig. 1, similar to FCC riser reactor.Tubular type is made charcoal, and to use cross sections be circular metal tube manufacture for device 25, liner insulating and wearing-resistant lining (figure slightly); Vertical height (from top to bottom) is generally 10～40m, and interior diameter is generally 400～5000mm.
The make charcoal housing of device 1 of bed formula is mainly comprised of superposed cylindrical metal cylindrical shell and the inverted round table face shape metal cylinder that is positioned at bottom, liner insulating and wearing-resistant lining (figure slightly).Bed formula is made charcoal in device 1 and is provided with cyclonic separator; Cyclonic separator shown in Fig. 1, for the dipleg of the 3rd cyclonic separator 18 that is installed in series and 19, two cyclonic separators of the 4th cyclonic separator stretches to bed formula, make charcoal in device dense bed 20 (stretch to bed formula make charcoal the top of device dense bed 20).The make charcoal top of device 1 of bed formula is provided with flue gas collection chamber 17 and smoke outlet tube 32, and bottom is provided with two sections of air-distributors 21 of making charcoal.The make charcoal overall structure of device 1 of the formula of bed shown in Fig. 1, similar to FCC revivifier.
The mixing device of described resinous shale raw material and high-temperature heat carrier is mixing tube 8.The outlet of mixing tube 8 passes in bed formula dry distillation reactor device 26, is generally the top that is positioned at bed formula dry distillation reactor device dense bed 27 interfaces; The entrance of mixing tube 8 is connected with the outlet of high-temperature heat carrier transfer lime 10 with the outlet of resinous shale material feeding tube 11.The entrance of high-temperature heat carrier transfer lime 10 passes into bed formula and makes charcoal in device 1, is positioned at the bed formula device dense bed 20 (be generally positioned at bed formula make charcoal middle part or the bottom of device dense bed 20 height) of making charcoal.High-temperature heat carrier transfer lime 10 is provided with high-temperature heat carrier flowrate control valve 5, with the flow of high-temperature heat carrier in control tube.
The make charcoal heat-obtaining discharger of device dense bed 20 interior high-temperature heat carriers of described bed formula comprises high-temperature heat carrier drainage conduit 6.The entrance of high-temperature heat carrier drainage conduit 6 and the bed formula device 1 of making charcoal is connected, and is to be generally connected in bed formula the make charcoal middle part of device dense bed 20 height or the position of bottom.The outlet of high-temperature heat carrier drainage conduit 6 is connected with the bottom of heat collector 4, and the top of heat collector 4 is connected with the top of thermal barrier blow-down drum 3 by pipeline 2.Heat collector 4 can be used various FCC external warmers, the water at the general environment for use temperature of heat-obtaining medium (figure slightly).Thermal barrier blow-down drum 3 is a metal vessel.High-temperature heat carrier drainage conduit 6 is provided with high-temperature heat carrier flowrate control valve 5, with the flow of high-temperature heat carrier in control tube.
Each pipeline in destructive distillation device, is all used cross section for circular metal tube, liner insulating and wearing-resistant lining (figure slightly).The interior diameter of each pipeline is mainly determined according to the flow of material and/or medium in each pipeline, density calculation.
High-temperature heat carrier flowrate control valve 5 and semicoke flowrate control valve 30, can use various conventional for controlling the flowrate control valve of solid powder/particle flow, as used guiding valve.Make charcoal air-distributor 28 and two sections of air-distributors 21 of making charcoal of stripped vapor sparger 7, one section can be used conventional annular sparger or dendroid sparger.
Adopt the destructive distillation device shown in Fig. 1 to carry out the method (referred to as method for destructive distillation) of oil shale fluidized bed dry distillation of the present invention, in turn include the following steps:
A. the resinous shale raw material 9 after pulverizing enters mixing tube 8 through resinous shale material feeding tube 11, and the high-temperature heat carrier that bed formula is made charcoal in device 1 enters mixing tube 8 through high-temperature heat carrier transfer lime 10.Resinous shale raw material 9 and high-temperature heat carrier be coflow transmission of heat by contact after the interior mixing of mixing tube 8, then enters bed formula dry distillation reactor device 26 by the outlet of mixing tube 8.Resinous shale raw material 9 carries out dry distillation reactor in bed formula dry distillation reactor device dense bed 27, generates shale oil, carbonization gas and shale semicockes.
Shale semicockes and thermal barrier in bed formula dry distillation reactor device dense bed 27 are mixed to form mixing semicoke mutually.The oil gas 23 that dry distillation reactor generates, also have at the interior stripping of stripping stage 14 and mix the oil gas that mixing semicoke that half defocused water vapor and stripping go out is carried secretly, it is defocused that the first cyclonic separator 12 in being located at bed formula dry distillation reactor device 26 and the second cyclonic separator 13 are isolated mixing half together, by oil gas collection chamber 24 and oil gas vent pipe 31, by the top of bed formula dry distillation reactor device 26, flowed out, enter fractionating system and carry out fractionation (embodiment 1～embodiment 7 herewith; Figure slightly).Described oil gas, refers to shale oil and carbonization gas that dry distillation reactor generates.The first cyclonic separator 12 and the isolated mixing semicoke of the second cyclonic separator 13, in dipleg falls into bed formula dry distillation reactor device dense bed 27.
Mixing semicoke in bed formula dry distillation reactor device dense bed 27 flows downward, and enters the stripping stage 14 of being located at bed formula dry distillation reactor device 26 belows.Through stripped vapor sparger 7, in stripping stage 14, pass into water stripping steam 71, stripping goes out to mix semicoke entrained oil gas.Mixing semicoke after the interior stripping of stripping stage 14 flows to the bottom (Figure 1 shows that bottom) of stripping stage 14, through semicoke transfer lime 15, enters the make charcoal bottom of device 25 of tubular type.
B. enter the mixing semicoke that tubular type makes charcoal in device 25 and contact with one section that is passed into by one section of air-distributor 28 of the making charcoal air 29 (pressurized air) of making charcoal, along tubular type, making charcoal, device 25 is up to carry out one section and makes charcoal.
C. one section of mixing semicoke after making charcoal enters the bed formula device 1 of making charcoal together with one section of flue gas of generating of making charcoal by the make charcoal outlet of device 25 of tubular type.Wherein one section of mixing semicoke after making charcoal is made charcoal in device dense bed 20 to falling into bed formula, in bed formula is made charcoal device dense bed 20, contact with two sections of air 22 of making charcoal that passed into by two sections of air-distributors 21 of making charcoal and carry out two sections and make charcoal, remaining coke on burning-off mixing semicoke, generates high-temperature heat carrier.
Make charcoal and two sections of flue gases 16 of generating of making charcoal are isolated after high-temperature heat carrier through the 3rd cyclonic separator 18 and the 4th cyclonic separator 19 being located at bed formula and making charcoal in device 1 for one section, by flue gas collection chamber 17 and smoke outlet tube 32, by the make charcoal top of device 1 of bed formula, discharged.The 3rd cyclonic separator 18 and the isolated high-temperature heat carrier of the 4th cyclonic separator 19, fall into bed formula through dipleg and make charcoal in device dense bed 20.
The high-temperature heat carrier that bed formula is made charcoal in device dense bed 20 is flowed out by the bed formula device 1 of making charcoal, and a part is discharged destructive distillation device after heat-obtaining cooling.Referring to Fig. 1, a part of high-temperature heat carrier enters heat collector 4 through high-temperature heat carrier drainage conduit 6, by heat-obtaining medium heat-obtaining cooling (be normally cooled to below 100 ℃, become Low Temperature Thermal carrier).After the cooling of high-temperature heat carrier heat-obtaining, by pipeline 2, enter thermal barrier blow-down drum 3, finally by thermal barrier blow-down drum 3, discharge destructive distillation device (can be used as material of construction uses).The present invention discharges a part of high-temperature heat carrier the amount of destructive distillation device, according to the material balance calculative determination of destructive distillation device.
By the bed formula high-temperature heat carrier that another part bed formula that device 1 flows out makes charcoal in device dense bed 20 of making charcoal, in high-temperature heat carrier transfer lime 10 enters mixing tube 8, mix with resinous shale raw material 9.
Above-mentioned steps A～C continuously, loop.
The operational condition of above-mentioned method for destructive distillation is generally as follows:
In step B, enter mixing semicoke that tubular type makes charcoal in device 25 after one section is made charcoal, by the coke of burning-off 30%～70%; By the weight percentage of burning-off coke, equal to mix one section of semicoke make charcoal before and after the difference of contained weight of coke percentage ratio divided by the weight percentage of (after being stripping) contained coke before mixing one section of semicoke and making charcoal, then be multiplied by 100%.In tubular type is made charcoal device 25, also burn the remaining oil gas of carrying secretly of mixing semicoke after stripping.
In steps A, the high-temperature heat carrier entering in mixing tube 8 is 2～7 with the ratio of the weight rate of resinous shale raw material 9; The make charcoal temperature identical (embodiment 1～embodiment 7 herewith) of device dense bed 20 of the temperature of described high-temperature heat carrier and bed formula is 650～750 ℃.
In steps A, the dry distillation reactor time of resinous shale raw material 9 in bed formula dry distillation reactor device dense bed 27 is 2～10min, the temperature (being dry distillation reactor temperature) of bed formula dry distillation reactor device dense bed 27 is 450～550 ℃, the linear gas velocity of bed formula dry distillation reactor device 26 dilute phase sections is 0.1～0.8m/s, and the absolute pressure at bed formula dry distillation reactor device 26 tops is 0.1～0.4MPa.The dilute phase section of bed formula dry distillation reactor device 26, refers to the section that is positioned at bed formula dry distillation reactor device dense bed 27 tops, interface.Described gas, is mainly included in the interior stripping of stripping stage 14 and mixes the oil gas that the interior dry distillation reactor of oil gas, bed formula dry distillation reactor device dense bed 27 that half defocused water vapor, mixing semicoke that stripping goes out carry secretly generates.In operating process, bed formula dry distillation reactor device dense bed 27 is in inflation fluidized state.
The dry distillation reactor time of resinous shale raw material 9 in bed formula dry distillation reactor device dense bed 27 is 3～6min preferably, preferably 470～530 ℃ of the temperature of bed formula dry distillation reactor device dense bed 27.
The dry distillation reactor time of resinous shale raw material 9 in bed formula dry distillation reactor device dense bed 27 is preferably 3.5～4.5min, and the temperature of bed formula dry distillation reactor device dense bed 27 is preferably 490～510 ℃.
The interior diameter of bed formula dry distillation reactor device 26 top cylinder shape cylindrical shells is mainly according to the mobility scale calculative determination of bed formula dry distillation reactor device 26 dilute phase section linear gas velocities, the height of bed formula dry distillation reactor device dense bed 27 is the reserve calculative determination of the dry distillation reactor time in bed formula dry distillation reactor device dense bed 27 and bed formula dry distillation reactor device 26 interior mixing semicokes according to resinous shale raw material 9 mainly, and the height of bed formula dry distillation reactor device 26 dilute phase sections is mainly according to the settling height calculative determination that mixes semicoke.
The present invention uses bed formula dry distillation reactor device 26, and the complexity that its operation is controlled is lower.And, at the interior stripping of stripping stage 14, mix the oil gas that the interior dry distillation reactor of oil gas, bed formula dry distillation reactor device dense bed 27 that half defocused water vapor, mixing semicoke that stripping goes out carry secretly generates, can make bed formula dry distillation reactor device dense bed 27 in inflation fluidized state as fluidizing medium, do not need to use dry gas, so the energy consumption of bed formula dry distillation reactor device 26 is lower.In addition, bed formula can keep comparatively stablely in the temperature of heating up in a steamer reactor dense bed 27.
In steps A, the temperature of the interior mixing semicoke of stripping stage 14 bed is 480～520 ℃.Enter mixing semicoke in stripping stage 14 after stripping, conventionally can stripping go out and more than 95% carry oil gas (embodiment 1～embodiment 7 herewith) secretly.The coke content of the mixing semicoke after the interior stripping of stripping stage 14, is generally 3%～15%.
In step B, entering mixing semicoke that tubular type makes charcoal in device 25, in tubular type is made charcoal device 25, to carry out one period of making charcoal be 5～40s; The make charcoal temperature in device 25 exits of tubular type is 600～750 ℃, and absolute pressure is 0.1～0.4MPa; The average air linear speed that tubular type is made charcoal in device 25 is that this average air linear speed of 1～10m/s[refers to that one section of air 29 of making charcoal enters the tubular type backward mobile average linear speed within device 25 (calculating under tubular type is made charcoal the temperature in device 25 exits and absolute pressure condition) of making charcoal].Tubular type the make charcoal absolute pressure basic identical (embodiment 1～embodiment 7 herewith) at device 1 top of the absolute pressure in device 25 exits and bed formula of making charcoal.Tubular type is made charcoal the vertical height of device 25 mainly according to the make charcoal total height calculative determination of device 1 of its operational condition and bed formula dry distillation reactor device 26, stripping stage 14 and bed formula, and interior diameter is mainly according to the mobility scale calculative determination of average air linear speed.
In step C, it is 3～6min that one section of mixing semicoke after making charcoal carries out two periods of making charcoal in bed formula is made charcoal device dense bed 20, the make charcoal temperature (i.e. two sections of charcoal temperatures) of device dense bed 20 of bed formula is 650～750 ℃, the make charcoal linear gas velocity of device 1 dilute phase section of bed formula is 0.2～1.2m/s, and the make charcoal absolute pressure at device 1 top of bed formula is 0.1～0.4MPa.The make charcoal dilute phase section of device 1 of bed formula, refers to and is positioned at the make charcoal section of device dense bed 20 tops, interfaces of bed formula.Described gas, is mainly one section and makes charcoal and two sections of flue gases of making charcoal and generating.In operating process, bed formula is made charcoal device dense bed 20 in inflation fluidized state.
Bed formula is made charcoal the interior diameter of device 1 top cylinder shape cylindrical shell mainly according to the make charcoal mobility scale calculative determination of device 1 dilute phase section linear gas velocity of bed formula, the bed formula height of the device dense bed 20 mixing semicoke after mainly making charcoal according to a section of making charcoal carries out the make charcoal reserve calculative determination of device 1 interior high-temperature heat carrier of two periods of making charcoal and bed formula in bed formula is made charcoal device dense bed 20, and bed formula is made charcoal the height of device 1 dilute phase section mainly according to the settling height calculative determination of high-temperature heat carrier.Mixing semicoke after the interior stripping of stripping stage 14 is interior after two sections are made charcoal at tubular type device 25, the bed formula device 1 of making charcoal of making charcoal, conventionally can more than 95% coke of burning-off.
The resinous shale raw material 9 that method for destructive distillation of the present invention is used is granular, and particle diameter is not more than 3mm (method of sieving measurement), and oleaginousness is 5%～35% (aluminium rice steamer method mensuration), and water content is not higher than 20%.
Technique described in CN101440293A, resinous shale raw material particle size is large (being less than 30mm); Although can reduce the Crashing Costs of resinous shale raw material, there are the following problems: 1. make the yield of shale oil reduce; 2. cause fluidisation and the difficulty of transportation of resinous shale raw material in destructive distillation device, be unfavorable for the maximization construction of destructive distillation device; 3. in fluidized bed dry distillation chamber, make the hot fluidizing medium of destructive distillation produce channel, bias current, cause resinous shale raw material to conduct heat inhomogeneous, and affect the destructive distillation effect of resinous shale raw material and the quality of the shale oil generating.For this technique, the technique described in the document 1 that this specification sheets is quoted is used particle diameter to be not more than the resinous shale raw material of 3mm, comparatively suitable.The present invention also uses the resinous shale raw material 9 of this particle diameter, can make like this resinous shale raw material 9 normally fluidisation and destructive distillation in bed formula dry distillation reactor device 26, improves the yield of shale oil; The coke that can also make to mix on semicoke when making charcoal for one section, two sections burns better simultaneously, thereby reclaims more heat.Use particle diameter to be not more than the resinous shale raw material 9 of 3mm, under operational condition of the present invention, shale oil yield can account for 75%～88% (shale oil yield of the present invention is the yield of actual acquisition) of resinous shale raw material 9 oleaginousness.
According to explanation of the present invention or requirement, the destructive distillation operational condition that the technician in oil shale distillation field can select the present invention to propose depending on concrete operations situation, selects various device member, carries out design, operation and the control of destructive distillation device.
The present invention, the temperature that enters the resinous shale raw material 9 of resinous shale material feeding tube 11 is envrionment temperature, one section of make charcoal air 29 and two sections of pressurized air (embodiment 1～embodiment 7 herewith) that the air 22 of making charcoal all forms for the air compressing by under envrionment temperature.Envrionment temperature of the present invention is 25～35 ℃, and pressure is absolute pressure, and percentage ratio is weight percentage, and interior diameter all refers to the interior diameter of the insulating and wearing-resistant lining of metal cylinder or pipe lining.In Fig. 1, the arrow of unreceipted Reference numeral represents the flow direction of various materials and/or medium.
Embodiment
On the small test device of the device of fluidized bed dry distillation shown in Fig. 1, by the step of the described dry distillation method of oil shale of this specification sheets embodiment part, carry out 7 groups of tests (embodiment 1～embodiment 7).Resinous shale raw material 9 all adopts cananga oil shale powder raw material, and character is in Table 1; Inlet amount (entering the weight rate of the resinous shale raw material 9 of resinous shale material feeding tube 11) is 150kg/ days.
In embodiment 1～embodiment 7, the linear gas velocity of bed formula dry distillation reactor device 26 dilute phase sections is 0.6m/s.The temperature of the interior mixing semicoke of stripping stage 14 bed is 500 ℃, and stripping medium is the water stripping steam 71 of 500 ℃.Through high-temperature heat carrier drainage conduit 6, enter the high-temperature heat carrier of heat collector 4, all by heat-obtaining medium (water under envrionment temperature) heat-obtaining, be cooled to 100 ℃.One section of make charcoal air 29 and two sections of air 22 of making charcoal are the pressurized air of 0.4MPa (absolute pressure), and test ambient temperature is 25～28 ℃.
The character of embodiment 1～embodiment 7 remaining operational condition, product distribution and portioned product, respectively in Table 2～table 8.Product in table 2～table 8 distributes, and all refers to that the total product of destructive distillation device distributes.In each embodiment, by the make charcoal coke content of the high-temperature heat carrier that device 1 flows out of bed formula, all identical in tubular type device 25 and the bed formula interior coke content through two sections of high-temperature heat carriers that generate after making charcoal of device 1 of making charcoal of making charcoal with the mixing semicoke after the interior stripping of stripping stage 14 described in table 2～table 8.After a part of high-temperature heat carrier heat-obtaining cooling described in table 2～table 8, discharge the ratio of destructive distillation device, all refer to that this part high-temperature heat carrier accounts for the percentage ratio of resinous shale raw material 9 weight rates that enter resinous shale material feeding tube 11 by make charcoal weight rate that device dense bed 20 flows out through high-temperature heat carrier drainage conduit 6 of bed formula.
The character of table 1 resinous shale raw material (embodiment 1～embodiment 7)
| Project | Data |
| Bulk specific gravity (sedimentation state), g/ml | 1.04 |
| Specific heat, cal/kg ℃ | 0.259 |
| Oleaginousness (aluminium rice steamer method mensuration), % | 8.5 |
| Water content, % | 6.9 |
| Ash oontent (combustion method mensuration), % | 70.4 |
| Size distribution, % | |
| Below 20 μ m | 16.5 |
| 20～ |
6 |
| 40～80μm | 5.1 |
| 80～110μm | 2.3 |
| 110～149μm | 3.1 |
| 149～500μm | 18.2 |
| 500～ |
20 |
| 1000～1500μm | 18.5 |
| 1500～3000μm | 10.3 |
The character of the operational condition of table 2 embodiment 1, product distribution and portioned product
[note]: embodiment 2～embodiment 7 herewith.
The character of the operational condition of table 3 embodiment 2, product distribution and portioned product
The character of the operational condition of table 4 embodiment 3, product distribution and portioned product
The character of the operational condition of table 5 embodiment 4, product distribution and portioned product
The character of the operational condition of table 6 embodiment 5, product distribution and portioned product
The character of the operational condition of table 7 embodiment 6, product distribution and portioned product
The character of the operational condition of table 8 embodiment 7, product distribution and portioned product
Claims (5)
1. a fluidized bed dry distillation method for resinous shale, is characterized in that: the method in turn includes the following steps:
A. the resinous shale raw material (9) after pulverizing enters mixing tube (8) through resinous shale material feeding tube (11), the high-temperature heat carrier that bed formula is made charcoal in device (1) enters mixing tube (8) through high-temperature heat carrier transfer lime (10), outlet by mixing tube (8) after resinous shale raw material (9) and high-temperature heat carrier mix in mixing tube (8) enters bed formula dry distillation reactor device (26), resinous shale raw material (9) carries out dry distillation reactor in bed formula dry distillation reactor device dense bed (27), generate shale oil, carbonization gas and shale semicockes, shale semicockes and thermal barrier in bed formula dry distillation reactor device dense bed (27) are mixed to form mixing semicoke mutually, the cyclonic separator of the oil gas (23) that dry distillation reactor generates through being located at bed formula dry distillation reactor device (26) in isolates that mixing half is defocused is flowed out by bed formula dry distillation reactor device (26), mixing semicoke in bed formula dry distillation reactor device dense bed (27) flows downward, enter the stripping stage (14) of being located at bed formula dry distillation reactor device (26) below, in stripping stage (14), pass into water stripping steam (71), stripping goes out to mix semicoke entrained oil gas, mixing semicoke in stripping stage (14) after stripping flows to the bottom of stripping stage (14), through semicoke transfer lime (15), enter the make charcoal bottom of device (25) of tubular type,
B. enter the mixing semicoke that tubular type makes charcoal in device (25) and contact with one section of air of making charcoal (29), along tubular type, making charcoal, device (25) is up to carry out one section and makes charcoal;
C. one section of mixing semicoke after making charcoal enters the bed formula device (1) of making charcoal by the make charcoal outlet of device (25) of tubular type, in bed formula is made charcoal device dense bed (20), contact with two sections of air of making charcoal (22) and carry out two sections and make charcoal, remaining coke on burning-off mixing semicoke, generate high-temperature heat carrier, one section make charcoal and two sections make charcoal the flue gas (16) that generates after the cyclonic separator of being located at bed formula and making charcoal in device (1) is isolated high-temperature heat carrier by device (1) discharge of making charcoal of bed formula, the high-temperature heat carrier that bed formula is made charcoal in device dense bed (20) is flowed out by the bed formula device (1) of making charcoal, a part is discharged destructive distillation device after heat-obtaining cooling, another part is in high-temperature heat carrier transfer lime (10) enters mixing tube (8), mix with resinous shale raw material (9).
2. the fluidized bed dry distillation method of resinous shale according to claim 1, is characterized in that: enter mixing semicoke that tubular type makes charcoal in device (25) after one section is made charcoal, by the coke of burning-off 30%～70%.
3. the fluidized bed dry distillation method of resinous shale according to claim 1 and 2, it is characterized in that: the ratio that enters the weight rate of the interior high-temperature heat carrier of mixing tube (8) and resinous shale raw material (9) is 2～7, the dry distillation reactor time of resinous shale raw material (9) in bed formula dry distillation reactor device dense bed (27) is 2～10min, the temperature of bed formula dry distillation reactor device dense bed (27) is 450～550 ℃, the linear gas velocity of bed formula dry distillation reactor device (26) dilute phase section is 0.1～0.8m/s, the absolute pressure at bed formula dry distillation reactor device (26) top is 0.1～0.4MPa, entering mixing semicoke that tubular type makes charcoal in device (25), in tubular type is made charcoal device (25), to carry out one period of making charcoal be 5～40s, the make charcoal temperature in device (25) exit of tubular type is 600～750 ℃, absolute pressure is 0.1～0.4MPa, the average air linear speed that tubular type is made charcoal in device (25) is 1～10m/s, it is 3～6min that one section of mixing semicoke after making charcoal carries out two periods of making charcoal in bed formula is made charcoal device dense bed (20), the make charcoal temperature of device dense bed (20) of bed formula is 650～750 ℃, the make charcoal linear gas velocity of device (1) dilute phase section of bed formula is 0.2～1.2m/s, the make charcoal absolute pressure at device (1) top of bed formula is 0.1～0.4MPa.
4. the fluidized bed dry distillation method of resinous shale according to claim 1 and 2, is characterized in that: the particle diameter of resinous shale raw material (9) is not more than 3mm, and oleaginousness is 5%～35%, and water content is not higher than 20%, and percentage ratio is wherein weight percentage.
5. one kind for realizing the fluidized bed dry distillation device of the resinous shale of method described in claim 1, comprise a bed formula dry distillation reactor device (26), the bed formula device (1) of making charcoal, the mixing device that also has resinous shale raw material and high-temperature heat carrier, and with bed formula the make charcoal heat-obtaining discharger of the interior high-temperature heat carrier of device dense bed (20) of bed formula that device (1) is connected of making charcoal, it is characterized in that: the fluidized bed dry distillation device of resinous shale is also provided with the tubular type device (25) of making charcoal, bed formula dry distillation reactor device (26) is located at the make charcoal below of device (1) of bed formula, in bed formula dry distillation reactor device (26), be provided with cyclonic separator, the top of bed formula dry distillation reactor device (26) is provided with oil gas collection chamber (24) and oil gas vent pipe (31), below is provided with stripping stage (14), stripping stage is provided with stripping baffles in (14), stripped vapor sparger (7), the bottom of stripping stage (14) is provided with semicoke transfer lime (15), which is provided with semicoke flowrate control valve (30), the make charcoal bottom of device (25) of the outlet of semicoke transfer lime (15) and tubular type is connected, the make charcoal bottom of device (25) of tubular type is provided with one section of air-distributor of making charcoal (28), the make charcoal outlet of device (25) of tubular type passes into bed formula and makes charcoal in device (1), bed formula is made charcoal in device (1) and is provided with cyclonic separator, the make charcoal top of device (1) of bed formula is provided with flue gas collection chamber (17) and smoke outlet tube (32), bottom is provided with two sections of air-distributors of making charcoal (21), the mixing device of described resinous shale raw material and high-temperature heat carrier is mixing tube (8), the outlet of mixing tube (8) passes in bed formula dry distillation reactor device (26), the entrance of mixing tube (8) is connected with the outlet of high-temperature heat carrier transfer lime (10) with the outlet of resinous shale material feeding tube (11), the entrance of high-temperature heat carrier transfer lime (10) passes into bed formula and makes charcoal in device (1), the make charcoal heat-obtaining discharger of the interior high-temperature heat carrier of device dense bed (20) of described bed formula comprises high-temperature heat carrier drainage conduit (6), the entrance of high-temperature heat carrier drainage conduit (6) and the bed formula device (1) of making charcoal is connected, outlet is connected with heat collector (4), heat collector (4) is connected with thermal barrier blow-down drum (3) by pipeline (2), in high-temperature heat carrier transfer lime (10) and high-temperature heat carrier drainage conduit (6), be equipped with high-temperature heat carrier flowrate control valve (5).
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080290000A1 (en) * | 2007-05-22 | 2008-11-27 | Towler Gavin P | Coking Apparatus and Process for Oil-Containing Solids |
| CN101358136A (en) * | 2008-10-07 | 2009-02-04 | 中国石油大学(北京) | Method for directly fluid coking oil sand and apparatus |
-
2011
- 2011-12-05 CN CN201110413811.0A patent/CN103131447B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080290000A1 (en) * | 2007-05-22 | 2008-11-27 | Towler Gavin P | Coking Apparatus and Process for Oil-Containing Solids |
| CN101358136A (en) * | 2008-10-07 | 2009-02-04 | 中国石油大学(北京) | Method for directly fluid coking oil sand and apparatus |
Non-Patent Citations (2)
| Title |
|---|
| 油页岩固体热载体流化干馏炼油工艺中试研究;王伟东等;《煤化工》;20090630(第3期);19-22页 * |
| 王伟东等.油页岩固体热载体流化干馏炼油工艺中试研究.《煤化工》.2009,(第3期),19-22页. |
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