CN103571511B - Powder coal dry distillation method and device - Google Patents
Powder coal dry distillation method and device Download PDFInfo
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- CN103571511B CN103571511B CN201210276895.2A CN201210276895A CN103571511B CN 103571511 B CN103571511 B CN 103571511B CN 201210276895 A CN201210276895 A CN 201210276895A CN 103571511 B CN103571511 B CN 103571511B
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Abstract
The invention discloses a powder coal dry distillation method and device, and aims to solve the problems that the technical process is, the circulation amount of the solid heat carrier is high, the gas heat carrier needs to be delivered by a gas compressor and the like in the existing powder coal dry distillation technique. The dry distillation method comprises the following steps: A. a powder coal raw material (2), and a high-temperature solid heat carrier and a high-temperature oxygen-free flue gas from a tubular charcoal burner (7) are mixed in a mixing heat transfer region to perform contact heat transfer, and are subject to dry distillation reaction; B. after entrained oil gas is stripped out from semicoke formed in the step A in a stripping section (17), part of the semicoke is cooled and discharged out of the dry distillation device, and the other part enters the tubular charcoal burner; and C. the semicoke entering the tubular charcoal burner contacts charcoal burning air to perform charcoal burning, thereby generating the high-temperature solid heat carrier and high-temperature oxygen-free flue gas. The invention also discloses a powder coal dry distillation device for implementing the dry distillation method. The method and device can be used for dry distillation processing of various types of powder coal.
Description
Technical field
The invention belongs to fine coal retorting technique field, relate to a kind of method for destructive distillation and device of fine coal.
Background technology
Along with the arrival of scarcity and the Waste Era of Oil day by day of world petroleum resource, countries in the world utilize dry distillation of coal technology to produce coal tar, become alternative, have supplemented the important aspect of petroleum resources.The product of the dry distillation of coal is semicoke, oil gas (mainly coal tar and liquefied gas) and coal gas; The productive rate of dry distillation of coal product and composition depend on feed coal character, processing conditions (mainly temperature and time).
The fine coal method for destructive distillation that " brown coal hot solid carrier devolatilization new technology type approval test " literary composition that " Journal of Dalian University of Technology Total " February nineteen ninety-five the 1st, periodical was stepped on is introduced, feed coal is crushed to be less than 6mm, with after heat smoke lifting also heat drying in dry riser tube, dry coal enters dry coal storage tank, then removes mixing tank through feeding machine.The 800 DEG C of hot coke powders carrying out self-heating semicoke storage tank mix with dry coal mutually at mixing tank, and after mixing, the temperature of material is 550 ~ 650 DEG C; Then enter reactor, complete the fast pyrogenation reaction of coal, separate out destructive distillation gaseous product.Coal or semi-coke powder, at the oxygen gas of fluidized bed combustion stove burning generation 800 ~ 900 DEG C, to burn with the 600 DEG C of semicoke generating portions carrying out autoreactor in heater riser tube bottom and by heater riser to hot semicoke storage tank; Coke powder is heated to 800 ~ 850 DEG C, recycles as thermal barrier (solid).Dry riser tube is removed by hot semicoke storage tank heat smoke out.Reactor lower part by product semicoke pipe export section coke powder, through overcooling, as semicoke product export.Aforesaid method Problems existing is: 1. burn with the semicoke generating portion carrying out autoreactor in heater riser tube with the oxygen gas that fluidized bed combustion stove produces, semicoke by heater riser to hot semicoke storage tank, hot coke powder enters mixing tank from hot semicoke storage tank again and mixes mutually with dry coal, enters reactor and react after mixing; This just makes technological process comparatively complicated.2. only use hot coke powder to heat dry coal as solid thermal carriers, make the internal circulating load of solid thermal carriers comparatively large, the throughput of semicoke product can be reduced; Generate a large amount of hot coke powders, energy consumption is also higher.
Chinese patent CN101328415A discloses a kind of piston type fluidized bed low temperature dry distillation technological process, utilize lifting tube flowing catalytic cracking device principle, take riser reactor as dry distillation reactor device, being high-temperature water gas producer with catalyst regenerator, take high-temperature water gas as fluidizing medium and the thermal barrier of destructive distillation raw material.Carry out dry distillation reactor by destructive distillation feedstock transportation to riser tube fluidized-bed reactor, the rear oil gas of reaction carries out separation and obtains retorted product.Pyrolysis Char enters water-gas machine, and the carbon in Pyrolysis Char, the oxygen in air and water vapor carry out being oxidized and water-gas reaction, obtain water-gas.Problems existing is: as the high-temperature water gas of destructive distillation raw material fluidizing medium and thermal barrier, need to be transported to riser tube dry distillation reactor device with gas compressor from water-gas machine.Conveying high-temperature water gas can propose higher material requirement to gas compressor; Gas compressor is in high harsh running condition all the time in addition, will have influence on the long-term operation of destructive distillation device.
Summary of the invention
The object of this invention is to provide a kind of method for destructive distillation and device of fine coal, the technological process that existing fine coal retorting technique exists respectively is comparatively complicated to solve, the internal circulating load of solid thermal carriers is comparatively large, gaseous heat-carrier needs to use the problems such as gas compressor conveying.
For solving the problem, the technical solution used in the present invention is:
A method for destructive distillation for fine coal, is characterized in that: the method in turn includes the following steps:
A. fine coal raw material enters dry distillation reactor device through fine coal material feeding tube, dry distillation reactor device is entered from the make charcoal high-temp solid thermal barrier of device and anaerobic flue gas of tubular type, fine coal raw material carries out mixing and transmission of heat by contact in the contact heat transfer region in dry distillation reactor device with high-temp solid thermal barrier and anaerobic flue gas, fine coal raw material carries out dry distillation reactor in dry distillation reactor device dense bed afterwards, generate water vapor, oil gas, coal gas and solid product, fine coal destructive distillation solid product in dry distillation reactor device dense bed and solid thermal carriers are mixed to form semicoke mutually, gas in dry distillation reactor device is isolated half through the cyclonic separator be located in dry distillation reactor device and defocusedly to be flowed out by dry distillation reactor device, semicoke in dry distillation reactor device dense bed flows downward, enter the stripping stage be located at below dry distillation reactor device,
B. in stripping stage, stripping steam is passed into, stripping goes out semicoke entrained oil gas, semicoke in stripping stage after stripping flows to the bottom of stripping stage, and a part discharges destructive distillation device after heat-obtaining cooling, and another part enters tubular type through semicoke transfer lime and to make charcoal the bottom of device;
C. enter the semicoke that tubular type makes charcoal in device to contact with the air of making charcoal passed into bottom device of making charcoal from tubular type, making charcoal along tubular type, device is up makes charcoal, generate high-temp solid thermal barrier and anaerobic flue gas, high-temp solid thermal barrier and anaerobic flue gas enter in dry distillation reactor device, mix with fine coal raw material.
For realizing the fine coal destructive distillation device of aforesaid method, comprise dry distillation reactor device, thermal barrier generating apparatus, it is characterized in that: dry distillation reactor device is bed formula fluidized bed dry distillation reactor, thermal barrier generating apparatus is that the tubular type coaxially arranged with dry distillation reactor device is made charcoal device, dry distillation reactor device is provided with fine coal material feeding tube, the below of dry distillation reactor device is coaxially arranged with stripping stage with it, tubular type makes charcoal device through stripping stage, its top exit is positioned at the top at dry distillation reactor device dense bed interface, the below of fine coal material feeding tube outlet, the bottom of stripping stage is provided with semicoke drainage conduit and semicoke transfer lime, the outlet of semicoke drainage conduit is connected with heat collector, heat collector is connected with semicoke blow-down drum by pipeline, the make charcoal bottom of device of outlet and the tubular type of semicoke transfer lime is connected, the make charcoal bottom of device of tubular type is provided with air-distributor of making charcoal.
The present invention adopts fluidization to carry out fine coal destructive distillation; Adopt the present invention, there is following beneficial effect: (1) semicoke is made charcoal in tubular type makes charcoal device, the high-temp solid thermal barrier generated and high temperature anaerobic flue gas enter dry distillation reactor device, fine coal raw material enters dry distillation reactor device through fine coal material feeding tube, directly mix in dry distillation reactor device and transmission of heat by contact with above-mentioned high-temp solid thermal barrier and high temperature anaerobic flue gas, namely in dry distillation reactor device dense bed, dry distillation reactor is carried out subsequently, distillation process process is comparatively simple, and destructive distillation device structure is also fairly simple.(2) fine coal raw material is jointly heated with the high-temp solid thermal barrier of device of making charcoal from tubular type and high temperature anaerobic flue gas, the heat that anaerobic flue gas carries obtains effective utilization, thus consumption and the internal circulating load of solid thermal carriers can be reduced, increase the throughput of the higher semicoke product of value, increase economic efficiency.(3) consumption due to solid thermal carriers is less, so can reduce the energy consumption (comprise reduction make charcoal air consumption) generating high-temp solid thermal barrier.The make charcoal load of making charcoal of device of tubular type is lower, and its scantlings of the structure and investment can reduce; Charcoal temperature is easy to control, and can prevent overtemperature from damaging.Present invention uses tubular type to make charcoal device, it has stronger ability of making charcoal and better turndown ratio.(4) consumption of high-temp solid thermal barrier is less, the ratio of mixture lower (enter the high-temp solid thermal barrier of dry distillation reactor device and be generally 2.5 ~ 3.5 with the ratio of the weight rate of fine coal raw material) of itself and fine coal raw material, so just can improve the coke content of outer row's semicoke, thus improve the further utility value of semicoke product.(5) make charcoal to make charcoal in the device high temperature anaerobic flue gas that generates of tubular type is flowed out by the make charcoal outlet of device of tubular type, directly enters dry distillation reactor device and heat fine coal raw material together with high-temp solid thermal barrier.So the present invention does not need to use gas compressor conveying high temperature anaerobic flue gas, do not exist and the problem that higher material requires is proposed to gas compressor, there is not gas compressor yet and be in high harsh running condition all the time and the problem that has influence on destructive distillation device long-term operation.
The present invention can be used for the processing of various powder coal carbonization, is particularly useful for the processing of low grade coal (such as brown coal) powder coal carbonization.The destructive distillation course of processing can be carried out continuously, stably, flexible adjustment; Fine coal feed throughput is large, and coal tar yield is high.
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 fine coal destructive distillation device of the present invention.
Embodiment
See Fig. 1, fine coal destructive distillation device (referred to as destructive distillation device) of the present invention, comprises dry distillation reactor device 5, thermal barrier generating apparatus.Dry distillation reactor device 5 is bed formula fluidized bed dry distillation reactor, and thermal barrier generating apparatus is that the coaxial tubular type arranged is made charcoal device 7 with dry distillation reactor device 5.The housing of dry distillation reactor device 5 forms primarily of superposed cylindrical metal cylindrical shell and the inverted round table face shape metal cylinder being positioned at bottom, liner insulating and wearing-resistant lining (figure slightly).Cyclonic separator is provided with in dry distillation reactor device 5; Cyclonic separator shown in Fig. 1, for the dipleg of the first cyclonic separator 181 of being installed in series and the second cyclonic separator 182, two cyclonic separators stretches in dry distillation reactor device dense bed 6 (stretching to the top of dry distillation reactor device dense bed 6).The top of dry distillation reactor device 5 is provided with collection chamber 1 and gas outlet tube 19.Dry distillation reactor device 5 is provided with fine coal material feeding tube 3.
The below of dry distillation reactor device 5 is coaxially arranged with stripping stage 17 with it, the top of stripping stage 17 is connected with the bottom of dry distillation reactor device 5.The housing of stripping stage 17 forms primarily of a cylindrical metal cylindrical shell, liner insulating and wearing-resistant lining (figure slightly).Stripping baffles (shown in Fig. 1 is herring-bone stripping baffles), stripped vapor sparger 80 is provided with in stripping stage 17.Tubular type makes charcoal device 7 through stripping stage 17, and its top exit is positioned at the top at dry distillation reactor device dense bed interface 60, the below of fine coal material feeding tube 3 outlet.The device of dry distillation reactor shown in Fig. 1 5-stripping stage 17-tubular type is made charcoal the overall structure of device 7, similar to transfer line fluid cat cracking (FCC) device in refining of petroleum coaxial-type.
The bottom of stripping stage 17 is provided with semicoke drainage conduit 16 and semicoke transfer lime 9, it is equipped with semicoke flowrate control valve 10, with the flow of semicoke in control tube.In Fig. 1, the entrance of semicoke drainage conduit 16 is connected with the bottom of stripping stage 17, exports and is connected with the bottom of heat collector 14; The top of heat collector 14 is connected with the top of semicoke blow-down drum 13 by pipeline 15.Heat collector 14 can use various FCC external warmer, the de-salted water (needing above zero) at the general environment for use temperature of heat-obtaining medium 21.Semicoke blow-down drum 13 is a metal vessel.
The make charcoal bottom of device 7 of outlet and the tubular type of semicoke transfer lime 9 is connected.The make charcoal bottom of device 7 of tubular type is provided with air-distributor 11 of making charcoal, and air-distributor 11 of the making charcoal outlet of being located at semicoke transfer lime 9 and tubular type are made charcoal the below of interface that device 7 is connected.Tubular type shown in Fig. 1 is made charcoal the overall structure of device 7, similar to FCC riser reactor.Tubular type is made charcoal the metal tube manufacture that device 7 uses cross section to be circle, 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.
In Fig. 1, the make charcoal top of device 7 top exit of tubular type is provided with baffle plate 4, and effect directly rushes at tubular type after preventing fine coal raw material 2 from being flowed out by the outlet of fine coal material feeding tube 3 to make charcoal the top exit of device 7, causes the make charcoal top hole pressure of device 7 of tubular type to increase.Baffle plate 4 is generally cone surface shape (as shown in Figure 1) or circular flat shape (figure slightly), is fixed on tubular type makes charcoal the top of device 7 by metal rod.When baffle plate 4 is cone surface shape, its circular cone apex angle α (as shown in Figure 1) is generally 60 ~ 90 degree.
In Fig. 1, fine coal material feeding tube 3 is made up of with vertical pipeline section horizontal pipeline section, and horizontal pipeline section is fixed on the cylindrical drum on dry distillation reactor device 5 top.The top that the outlet of fine coal material feeding tube 3 is positioned at the bottom of vertical pipeline section, tubular type makes charcoal device 7 top exit and baffle plate 4.The vertical range H being exported to cone surface shape baffle plate 4 top of fine coal material feeding tube 3, or to the vertical range (figure slightly) of circular flat shape baffle plate 4 upper surface, be generally 0.5 ~ 2.5m.
In Fig. 1, semicoke transfer lime 9 is made up of vertical pipeline section and inclination pipeline section.Vertical pipeline section (as flooding stream pipe) stretches in stripping stage 17 by the bottom of stripping stage 17, and the top entry of vertical pipeline section is the entrance of semicoke transfer lime 9, is positioned at the bottom of stripping stage 17.The outlet of inclination pipeline section is the outlet of semicoke transfer lime 9, is connected with the make charcoal bottom of device 7 of tubular type.
Each pipeline in destructive distillation device, all uses the metal tube that cross section is circle, 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.
Semicoke flowrate control valve 10 can use the various conventional flowrate control valve for controlling solid powder/particle flow, as used guiding valve.Stripped vapor sparger 80, air-distributor 11 of making charcoal can use 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 fine coal destructive distillation of the present invention, in turn include the following steps:
A. fine coal raw material 2 enters dry distillation reactor device 5 through fine coal material feeding tube 3, enters dry distillation reactor device 5 from the make charcoal high-temp solid thermal barrier of device 7 and high temperature anaerobic flue gas of tubular type.Fine coal raw material 2 carries out mixing and transmission of heat by contact in the contact heat transfer region in dry distillation reactor device 5 with high-temp solid thermal barrier and high temperature anaerobic flue gas, fine coal raw material 2 carries out dry distillation reactor in dry distillation reactor device dense bed 6 afterwards, generates water vapor, oil gas, coal gas and solid product; Wherein the main component of coal gas is methane, carbonic acid gas, carbon monoxide, hydrogen etc.Above-mentioned contact heat transfer region, the region between dry distillation reactor device 5 top cylinder shape cylindrical shell horizontal section to the dry distillation reactor device dense bed interface 60 residing for outlet referring to fine coal material feeding tube 3.
Fine coal destructive distillation solid product in dry distillation reactor device dense bed 6 and solid thermal carriers are mixed to form semicoke mutually.Gas 20 in dry distillation reactor device 5 enters the dilute phase section of dry distillation reactor device 5, enter collection chamber 1 through being located at after semicoke isolated by the first cyclonic separator 181 in dry distillation reactor device 5 and the second cyclonic separator 182 together, then flowed out by the top of gas outlet tube 19 from dry distillation reactor device 5.Described gas 20, mainly comprise the anaerobic flue gas of the device 7 of making charcoal from tubular type entered in dry distillation reactor device 5, fine coal raw material 2 water vapor, oil gas, coal gas that in dry distillation reactor device dense bed 6, dry distillation reactor generates, also have the semicoke entrained oil gas gone out from the defocused stripping steam 81 of stripping half in stripping stage 17 and stripping; Described oil gas, mainly coal tar and liquefied gas.Also a small amount of coal gas can be generated in the process that semicoke after following step C stripping is made charcoal in tubular type makes charcoal device 7; Stripping steam that these coal gas and semicoke carry enters in dry distillation reactor device 5 in company with the high-temp solid thermal barrier generated and high temperature anaerobic flue gas through the make charcoal top exit of device 7 of tubular type, also counts described gas 20.
First cyclonic separator 181 and the isolated semicoke of the second cyclonic separator 182, fall in dry distillation reactor device dense bed 6 through dipleg.
Semicoke in dry distillation reactor device dense bed 6 flows downward, and enters the stripping stage 17 be located at below dry distillation reactor device 5.
B. in stripping stage 17, pass into stripping steam 81 through stripped vapor sparger 80, stripping goes out semicoke entrained oil gas.Semicoke in stripping stage 17 after stripping flows to the bottom of stripping stage 17, and a part discharges destructive distillation device after heat-obtaining cooling, and another part enters tubular type through semicoke transfer lime 9 and to make charcoal the bottom of device 7.
See Fig. 1, the semicoke after a part of stripping enters heat collector 14 through semicoke drainage conduit 16, by heat-obtaining medium 21 heat-obtaining cooling (being normally cooled to less than 80 DEG C).Semicoke after heat-obtaining cooling enters semicoke blow-down drum 13 by pipeline 15, finally discharges destructive distillation device by semicoke blow-down drum 13, as semicoke product.Semicoke product has higher coke content, can be used as the fuel of circular fluid bed, or is used as to produce the raw material for the synthesis of the synthetic gas of methyl alcohol.
Semicoke after a part of stripping is discharged the amount of destructive distillation device by the present invention, and the MaterialBalance Computation according to destructive distillation device is determined.
C. enter semicoke that tubular type makes charcoal in device 7 to contact with from being located at the air 12 of making charcoal that the tubular type air-distributor 11 of making charcoal of making charcoal bottom device 7 passes into, making charcoal along tubular type, device 7 is up makes charcoal, part of coke on burning-off semicoke, generates high-temp solid thermal barrier and high temperature anaerobic flue gas.High-temp solid thermal barrier and high temperature anaerobic flue gas are flowed out by the make charcoal top exit of device 7 of tubular type, enter in dry distillation reactor device 5, mix, restart steps A in contact heat transfer region with fine coal raw material 2 after the baffle plate 4 of cone surface shape changes flow direction.The present invention is used for the high-temperature heat carrier of the contact heat transfer region heating fine coal raw material 2 in dry distillation reactor device 5, is made up of the high-temp solid thermal barrier of above-mentioned generation tubular type makes charcoal device 7 in and high temperature anaerobic flue gas.The high-temp solid thermal barrier that flows out of the outlet of making charcoal device 7 from tubular type generates through making charcoal by entering make charcoal semicoke in device 7 of tubular type, the present invention to the coke content of high-temp solid thermal barrier without strict restriction.In above-mentioned coke combustion, also burn that the semicoke after stripping is remaining carries oil gas secretly.
Above-mentioned steps A ~ C is continuous, circulation is carried out.
In steps A, the gas 20 in dry distillation reactor device 5 enters fractionating system and is separated with absorbing-stabilizing system, obtain raw gas, liquefied gas and liquid coal tar after flowing out from dry distillation reactor device 5.Raw gas of the present invention, the coal gas generated primarily of dry distillation reactor in dry distillation reactor device dense bed 6 and tubular type are made charcoal the anaerobic flue gas and a small amount of coal gas composition of to make charcoal in device 7 and generating.Raw gas and liquefied gas removed in pressure-swing absorption apparatus nitrogen, in desulfurizer, after desulfurization, obtain coal gas and liquefied gas product again; Liquid coal tar after desulfurization, is obtained liquid coal-tar products in desulfurizer.Said process is that this area is commonly used, and embodiment 1 ~ embodiment 6 is identical with it, and detailed description is omitted.
Above-mentioned coal gas and liquefied gas product can be used as domestic fuel, and coal gas product also may be used for further synthesizing methanol or oil product.Liquid coal-tar products can carry out secondary processing, produces vehicle fuel.Product that dry distillation reactor of the present invention obtains composition and distribution are see the embodiment of the present invention (in embodiment 1 ~ embodiment 6 by liquid coal-tar products referred to as coal tar).
The operational condition of method for destructive distillation of the present invention is generally as follows:
In steps A, entering the high-temp solid thermal barrier in dry distillation reactor device 5 with the ratio of the weight rate of fine coal raw material 2 is 2.5 ~ 3.5, and entering the high temperature anaerobic flue gas in dry distillation reactor device 5 with the ratio of the weight rate of fine coal raw material 2 is 0.13 ~ 0.15.High-temp solid thermal barrier and the fine coal raw material 2 mixed temperature in contact heat transfer region in dry distillation reactor device 5 (refer to the medial temperature on horizontal plane near above dry distillation reactor device dense bed interface 60, embodiment 1 ~ embodiment 6 herewith) is 460 ~ 580 DEG C.Enter the high-temp solid thermal barrier of dry distillation reactor device 5 and the temperature of high temperature anaerobic flue gas and tubular type to make charcoal the temperature at device 7 top exit place, the temperature entering the fine coal raw material 2 of fine coal material feeding tube 3 is envrionment temperature.
In step, the absolute pressure at dry distillation reactor device 5 top is 0.1 ~ 0.35MPa, the temperature (i.e. dry distillation reactor temperature) of dry distillation reactor device dense bed 6 is 450 ~ 560 DEG C, the dry distillation reactor time of fine coal raw material 2 in dry distillation reactor device dense bed 6 is 2 ~ 10min, and the linear gas velocity of dry distillation reactor device 5 dilute phase section is 0.3 ~ 0.9m/s.The temperature of dry distillation reactor device dense bed 6, refers to the medial temperature of dry distillation reactor device dense bed 6.The dilute phase section of dry distillation reactor device 5, refers to the section being positioned at dry distillation reactor device 5 contact heat transfer overlying regions.Described gas, see above to the explanation of gas 20.
In operating process, dry distillation reactor device dense bed 6 is in fluidisation swelling state.Fine coal raw material 2 water vapor, oil gas, coal gas that in dry distillation reactor device dense bed 6, dry distillation reactor generates, also have the semicoke entrained oil gas gone out from the defocused stripping steam 81 of stripping half in stripping stage 17 and stripping, dry distillation reactor device dense bed 6 can be made to be in fluidisation swelling state as fluidizing medium.
The temperature of dry distillation reactor device dense bed 6 preferably 480 ~ 540 DEG C, the dry distillation reactor time preferably 3 ~ 6min of fine coal raw material 2 in dry distillation reactor device dense bed 6.
The temperature of dry distillation reactor device dense bed 6 is preferably 500 ~ 520 DEG C, and the dry distillation reactor time of fine coal raw material 2 in dry distillation reactor device dense bed 6 is preferably 3.5 ~ 4.5min.
The interior diameter of dry distillation reactor device 5 top cylinder shape cylindrical shell mainly calculates according to the mobility scale of fine coal feed throughput, dry distillation reactor device 5 dilute phase section linear gas velocity to be determined, the height of dry distillation reactor device dense bed 6 mainly calculates according to the reserve of semicoke in the dry distillation reactor time of fine coal raw material 2 in dry distillation reactor device dense bed 6 and dry distillation reactor device 5 to be determined, the height of dry distillation reactor device 5 dilute phase section mainly calculates according to the settling height of semicoke to be determined.
In stepb, in stripping stage 17, the temperature of semicoke bed is 480 ~ 520 DEG C.Enter semicoke in stripping stage 17 after stripping, usually can stripping go out more than 95% carry oil gas (embodiment 1 ~ embodiment 6 herewith) secretly.The coke content of the semicoke in stripping stage 17 after stripping, is generally 75% ~ 85%.
In step C, entering the time that semicoke that tubular type makes charcoal in device 7 carries out making charcoal in tubular type makes charcoal device 7 is 5 ~ 40s (s is second); The make charcoal temperature in device 7 exit of tubular type is 670 ~ 750 DEG C, and absolute pressure is substantially identical with the absolute pressure at dry distillation reactor device 5 top.The tubular type average air linear speed of making charcoal in device 7 is 2 ~ 10m/s, and this average air linear speed refers to that air 12 of making charcoal enters tubular type and to make charcoal the average linear speed (calculating under tubular type makes charcoal the temperature in device 7 exit and absolute pressure condition) of backward upper flowing within device 7.Make charcoal the pressurized air of air 12 for being preheated to 120 ~ 180 DEG C, absolute pressure is 0.25 ~ 0.4MPa.According to flow and the coke content of the semicoke entered after stripping that tubular type makes charcoal in device 7, control to pass into tubular type through air-distributor 11 of making charcoal to make charcoal the flow of the air 12 of making charcoal in device 7, can make semicoke in coke combustion, exhaust the oxygen of making charcoal in air 12, obtain high temperature anaerobic flue gas in the make charcoal exit of device 7 of tubular type.Anaerobic flue gas refers to that flue gas is substantially free of free state oxygen.Regulate and pass into tubular type and to make charcoal the flow of the air 12 of making charcoal in device 7, tubular type can also be controlled and to make charcoal the temperature in device 7 exit.
The make charcoal vertical height of device 7 of tubular type mainly calculates according to the total height of its operational condition and dry distillation reactor device 5 and stripping stage 17 and determines, interior diameter mainly calculates according to the mobility scale of average air linear speed to be determined.
The fine coal raw material 2 that method for destructive distillation of the present invention uses is granular, and particle diameter is not more than 5mm, and water content is not higher than 45%, and oleaginousness is 5% ~ 25%.Water content and oleaginousness Ge Jinfa (the lattice gold low-temperature pyrolysis test method of GB/T1341-2007 coal) measure (embodiment 1 ~ embodiment 6 herewith).Use particle diameter to be not more than the fine coal raw material 2 of 5mm, can make fine coal raw material 2 can normally fluidisation and destructive distillation in bed formula dry distillation reactor device 5, obtain higher coal tar yield; Semicoke fluidisation in tubular type makes charcoal device 7 after simultaneously can also making stripping obtains better, coke on semicoke burns better, thus generates more heat.
Adopt destructive distillation device of the present invention and method for destructive distillation, higher coal tar yield can be obtained; The actual coal tar yield obtained, can reach 85% ~ 105% of fine coal raw material 2 oleaginousness measured by Ge Jinfa.
According to explanation of the present invention or requirement, the retorting operation condition that the technician in fine coal destructive distillation field can select the present invention to propose depending on concrete operations situation, selects various element of installation, carries out the design of destructive distillation device, operation and control.
Envrionment temperature of the present invention is-10 ~ 40 DEG C, 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 material and/or medium.
Embodiment
On the small test device of the destructive distillation device of fine coal shown in Fig. 1, carry out 6 groups of tests (embodiment 1 ~ embodiment 6) by the step of the fine coal method for destructive distillation described in this specification sheets embodiment part.Fine coal raw material 2 all adopts Yima fine coal raw material, and character is in table 1; Inlet amount (entering the weight rate of the fine coal raw material 2 of fine coal material feeding tube 3) is 3kg/h (3 kgs/hr).
In embodiment 1 ~ embodiment 6, in stripping stage 17, the temperature of semicoke bed is 520 DEG C, and stripping fluid is the stripping steam 81 of 520 DEG C.Semicoke after the stripping that semicoke drainage conduit 16 enters heat collector 14, is all cooled to 80 DEG C by heat-obtaining medium (de-salted water under envrionment temperature) heat-obtaining.The make charcoal absolute pressure in device 7 exit of tubular type is all substantially identical with the absolute pressure at dry distillation reactor device 5 top, and the test ambient temperature of each embodiment is see the temperature of fine coal raw material 2 in table 2.
Remaining operational condition of embodiment 1 ~ embodiment 6 is in table 2, and the character of product slates and portioned product is in table 3.Some projects in his-and-hers watches 3 are described as follows: 1. product slates, refer to the product slates that destructive distillation device is total.2. coal gas roughly by 40% methane, the carbonic acid gas of 20%, the carbon monoxide of 10%, and the composition such as the hydrogen of surplus, ethane and ethene.3. the main ingredient of liquefied gas is carbon 3, carbon 4.4. the stripping steam 81 passed in stripping stage 17 through stripped vapor sparger 80 is not counted in product slates.5. enter the tubular type oxygen of making charcoal in air 12 of making charcoal in device 7 through air-distributor 11 of making charcoal and count product slates (form with carbonic acid gas, carbon monoxide), the nitrogen of making charcoal in air 12 is not counted in product slates, and in air 12 of making charcoal, other gas seldom measured is not considered.
The character (embodiment 1 ~ embodiment 6) of table 1 fine coal raw material
| Project | Data |
| Bulk specific gravity (settling phase), g/ml | 1.06 |
| Specific heat, cal/kg DEG C | 0.264 |
| Oleaginousness, % | 12.5 |
| Water content, % | 20.5 |
| Coal ash content (combustion method mensuration), % | 13.4 |
| Size distribution, % | |
| Less than 20 μm | 6.5 |
| 20～40μm | 5.5 |
| 40～80μm | 6.6 |
| 80～110μm | 8.2 |
| 110～149μm | 10.3 |
| 149～500μm | 19.1 |
| 500～1000μm | 15.0 |
| 1000～1500μm | 13.3 |
| 1500～3000μm | 9.2 |
| 3000～5000μm | 6.3 |
The operational condition of table 2 embodiment 1 ~ 6
The product slates of table 3 embodiment 1 ~ 6 and the character of portioned product
Claims (4)
1. a fine coal destructive distillation device, comprise dry distillation reactor device (5), tubular type is made charcoal device (7), dry distillation reactor device (5) is provided with gas outlet tube (19), the make charcoal bottom of device (7) of tubular type is provided with air-distributor of making charcoal (11), it is characterized in that: dry distillation reactor device (5) is bed formula fluidized bed dry distillation reactor, make charcoal device (7) and dry distillation reactor device (5) of tubular type is coaxially arranged, dry distillation reactor device (5) is provided with fine coal material feeding tube (3), gas outlet tube (19) is located at the top of dry distillation reactor device (5), the top of dry distillation reactor device (5) is also provided with collection chamber (1), dry distillation reactor device is provided with cyclonic separator in (5), the below of dry distillation reactor device (5) is coaxially arranged with stripping stage (17) with it, tubular type makes charcoal device (7) through stripping stage (17), its top exit is positioned at the top at dry distillation reactor device dense bed interface (60), the below that fine coal material feeding tube (3) exports, the bottom of stripping stage (17) is provided with semicoke drainage conduit (16) and semicoke transfer lime (9), the outlet of semicoke drainage conduit (16) is connected with heat collector (14), heat collector (14) is connected with semicoke blow-down drum (13) by pipeline (15), the make charcoal bottom of device (7) of outlet and the tubular type of semicoke transfer lime (9) is connected.
2. device according to claim 1, is characterized in that: the make charcoal top of device (7) top exit of tubular type is provided with baffle plate (4), and baffle plate (4) is cone surface shape or circular flat shape.
3. device according to claim 1 and 2, is characterized in that: fine coal material feeding tube (3) is made up of with vertical pipeline section horizontal pipeline section, and the outlet of fine coal material feeding tube (3) is positioned at the bottom of vertical pipeline section.
4. device according to claim 1 and 2, it is characterized in that: semicoke transfer lime (9) is made up of vertical pipeline section and inclination pipeline section, vertical pipeline section stretches in stripping stage (17) by the bottom of stripping stage (17), the top entry of vertical pipeline section is the entrance of semicoke transfer lime (9), be positioned at the bottom of stripping stage (17), the outlet of inclination pipeline section is the outlet of semicoke transfer lime (9), is connected with the make charcoal bottom of device (7) of tubular type.
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