CN104099114A - Carbonization method for coal - Google Patents
Carbonization method for coal Download PDFInfo
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- CN104099114A CN104099114A CN201310136392.XA CN201310136392A CN104099114A CN 104099114 A CN104099114 A CN 104099114A CN 201310136392 A CN201310136392 A CN 201310136392A CN 104099114 A CN104099114 A CN 104099114A
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Abstract
The invention discloses a carbonization method for coal, which belongs to the field of the coal chemical industry. High temperature coal ash obtained after charking with a charking device and a tubular charking device is subjected to flue gas removal and then flows downwardly to enter a blending tank; the high temperature coal ash and a coal dust raw material entering the blending tank from a feed pipe undergo mixing and heat transfer; after the coal dust raw material and the high temperature coal ash undergo a mixing and heat transfer reaction via a delivery pipe, the coal dust raw material and the high temperature coal ash enter a carbonization reactor for a carbonization reaction; oil gas produced after the reaction is subjected to separation and stripping; the produced oil gas having undergone separation and stripping enters a fractionation system for fractionation; and a part of semicoke is discharged from an apparatus after heat removal, the other part of semicoke enters the charking device for charking, and regenerated semicoke obtained after charking goes upwardly via the tubular charking device for charking again and then enters a flue gas removal tower. With the charking system provided by the invention, cyclic, continuous and stable operation and flexible adjustment are realized, the content of NOX in flue gas discharged by the apparatus is greatly reduced, and the environment is protected.
Description
Technical field
The invention belongs to coal chemical technology, be specifically related to a kind of coal carbonization method.
Background technology
Along with the scarcity day by day of world petroleum resource and the arrival of Waste Era of Oil, countries in the world utilize dry distillation of coal technology to produce coal tar petroleum replacing resource has become important additional project.Carbon is most important component in coal. carbon content increases with the rising of degree of coalification, and peat is 50～60%; Brown coal are 60～77%; Bituminous coal is 74～92%; Hard coal is 90～98%.Hydrogen is second important component in coal. the hydrogen richness of sapropelinite is higher than humic coal, generally more than 6%, sometimes reaches 11%.Coal Chemical Industry be take the product of petroleum replacing chemical industry as main, as diesel oil, gasoline, aviation kerosene, liquefied petroleum gas (LPG), ethylene raw, pp material, alternative fuel (methyl alcohol, dme) etc., it is combined with the energy, Chemical Engineering Technology, can form the integrated new industry of coal-derived energy chemical.Coal Energy Source chemical industry will be played the part of important role in the sustainable use of China energy, is the important development direction of 20 years from now on, and this alleviates environmental pollution that fire coal causes, reduces China the dependence of Imported oil is all had great significance for China.
When the temperature of coal charge is during higher than 100 ℃, the moisture in coal evaporates; Temperature is elevated to 200 ℃ when above, in coal, in conjunction with water, disengages; When above up to 350 ℃, caking coal starts to soften, and further forms the plastic mass (this phenomenon does not occur for mud coal, brown coal etc.) of thickness; To 400～500 ℃ of most of dry gas and tar, separate out, claim one time thermal decomposition product; At 450～550 ℃, thermolysis is proceeded, residue retrogradation solidify to form semicoke gradually; Higher than 550 ℃, semicoke continues to decompose, and separates out remaining volatile matter (main component is hydrogen), and semicoke weightlessness is shunk simultaneously, forms crackle; Temperature is higher than 800 ℃, and the hardening of semicoke volume-diminished forms porous coke.When destructive distillation is carried out in cell-type gas retort, one time thermal decomposition product contacts with red-hot coke and high temperature furnace wall, second heat occurs and decompose, and forms second heat degradation production (coke-oven gas and other coking chemistry products).
The product of the dry distillation of coal is coal, coal tar and dry gas.The productive rate of dry distillation of coal product and composition depend on that raw material ature of coal, processing conditions are as temperature and time.Along with the difference of destructive distillation final temperature, dry distillation of coal product is also different.Low-temperature pyrolysis solid product is the black semicoke of short texture, and gas yield is low, and tar yield is high; High temperature carbonization solid product is the silver gray coke of compact structure, and dry gas yied is high and tar yield is low.The yield of medium temperature carbonization product, between low-temperature pyrolysis and high temperature carbonization.The dry gas main component generating in dry distillation of coal process is hydrogen and methane, can be used as fuel or industrial chemicals.High temperature carbonization is mainly for the production of metallurgical coke, and the tar of gained is the mixture of aromatic hydrocarbon, heterogeneous ring compound, is the important sources of industrial acquisition aromatic hydrocarbon; Low-temperature pyrolysis coal tar contains more alkane than high temperature tar, is one of artificial petroleum important sources.
Powder fluidized retorting technique is that lumped coal is pulverized as fine powder and high-temperature heat carrier (coal ash) are under fluidized state, directly, with the conduct heat process of concurrent heat-dissipating decomposition reaction of indirect contact, it is characterized by: coal dust destructive distillation hot strength is high, dry distillation rate soon, high, the gas-solid of coal tar productive rate can obtain sharp separation.
Lu Qi Rule Gas Company method (Lurgi Ruhrgas) by the Lurgi GmbH company of Germany and the Ruhrgas AG company development research of the U.S., its technical process is, after coal dust that granularity is less than to 5mm mixes with coke thermal barrier, in gravity moving-bed vertical reactor, to carry out destructive distillation.The coal gas and the tarry vapours that produce cause gas sweetening and coke tar recovery system, and the coke of circulation partly leaves pneumatic conveyor for upright furnace and promotes heating, separatedly with waste gas as thermal barrier, turn back to upright furnace afterwards again.Under normal pressure, carrying out pyrolysis, to obtain calorific value be 26～32MJ/m
3coal gas, semicoke and coal-based crude oil, to be tar products obtain through Hydrogenation the latter
The solid thermal carriers destructive distillation new technology of Dalian University of Technology's exploitation, its main experimental installation has mixing tank, reactive tank, fluidized bed combustion riser tube, aggregate groove and tar condensing recovery system etc.Feed coal adds raw material tank after pulverizing and being dried.The semicoke that destructive distillation produces is thermal barrier, is stored in aggregate groove, coal and semicoke by certain coking coal than entering mixing tank through material feeder respectively.Owing to mixing rapidly and evenly, raw meal particle size is little, and the semicoke of high temperature is passed to raw material particle by heat, and rate of heating is very fast, and coal Rapid Thermal occurs and decomposes.The volatile matter producing due to the pyrolysis of coal grain is drawn very fast, and secondary pyrolysis is lighter, therefore new distillation process coal tar productive rate is higher.
The CSIR O of Australia begins one's study by the method for quick coal pyrolyzing to obtain liquid fuel in 20 century 70s mid-term, successively set up 1g/h, 100g/h, the testing apparatus of tri-kinds of different scales of 20kg/h, has carried out thermal decomposition test to multiple bituminous coal, sub-bituminous coal, brown coal.The sand bed of this process using nitrogen fluidisation is reactor, and the coal dust (< 0.2m m) of pulverizing is sprayed into nitrogen in the sand bed of reactor, and rate of heating is about 104 ℃/s, and the main process of pyrolytic reaction completes in 1s.In addition pyrolytic tar has also been carried out to structural analysis, and carried out with several dissimilar reactors the research that hydrogenation of tar is processed.
A kind of piston type fluidized bed low temperature dry distillation technological process of coal dust that China Patent Publication No. CN 101328415 is related, utilize lifting tube flowing catalytic cracking device principle, the riser reactor of lifting tube flowing catalytic cracking device of take is dry distillation reactor device, the catalyst regenerator of lifting tube flowing catalytic cracking device of take is high-temperature water gas producer, fluidizing medium and thermal barrier that the high-temperature water gas of take is destructive distillation raw material, destructive distillation raw material is transported to the dry distillation reactor that carries out raw material in riser tube fluidized-bed reactor, the rear oil gas of reaction carries out separation and obtains destructive distillation product, Pyrolysis Char enters water-gas machine, carbon in Pyrolysis Char, airborne oxygen and water vapor are oxidized and water-gas reaction, the water-gas that reaction obtains is used as fluidizing medium and the thermal barrier of retort process, the solid lime-ash that Pyrolysis Char carries out after water-gas reaction is discharged.But this technique does not relate to the tubular type device of making charcoal makes charcoal and outer row's semicoke technology, and this Technology adopts high-temperature water gas circulation to have the following disadvantages as fluidizing medium and the thermal barrier of destructive distillation raw material: first, high-temperature gas circulation proposes higher material requirement to gas compressor; Secondly, the loop compression equipment of high-temperature gas, all the time in the harsh running condition of height, will affect the long-term operation of device.
The related a kind of low-temperature coal carbonization manufacturing technique technology principal character of China Patent No. 200610137759 is: feed coal, through coal bunker, blowing cylinder, auxiliary coal bin, enters furnace roof portion gas-collecting arrayed umbrella and carries out sub-material; Then enter dryer section, after drying section preheats, enter retort section, 100 ℃-550 ℃ of operating temperatures, move approximately 4 hours, and Heating Zone Temperature regulates and controls between 700-800 ℃, and semicoke fugitive constituent is dropped to below 6%; Then enter cooling section, high temperature semicoke cools by water-cooling jacket coke discharge box.The heat that this invention joins in stove is fully absorbed by coal, the destructive distillation time is short, directly rapidly, adopt large cavity design simultaneously, the even supply heated air of furnace bottom grid wall, makes gas retort treatment capacity improve 3 times of above and homogeneous heating compared with internal combustion external-heat stove, and temperature is controlled lower, tar yield is improved, by the former rate of recovery, below 50%, bring up to present more than 80%.But this technique does not relate to the tubular type device of making charcoal makes charcoal and powder fluidized bed retorting technique.The coal raw material granularity of this technology is 20～120mm, and dry and destructive distillation needs 4 hours, so will seriously restrict the maximization plant construction that adopts this technology.
Above-mentioned domestic and international coal dust destructive distillation does not all relate to the tubular type device of making charcoal makes charcoal and heating raw technology, and technological process is also different.In addition, above-mentioned technology does not all relate to NO in reduction discharge flue gas
xthe problem of content.
Summary of the invention
For solve the existing device of making charcoal of existing coal dust destructive distillation device make charcoal the large and temperature of load cannot flexible and control, the technical problems such as outer row's semicoke content exhaust gas volumn low, the generation of making charcoal is large, apparatus structure is complicated, the invention provides a kind of coal carbonization method, adopted make charcoal device and tubular type make charcoal device in conjunction with heating the coal dust raw material from feed-pipe, the high temperature coal ash of generation is high containing charcoal semicoke technology as the supplemental heat source of coal dust destructive distillation, outer row.By can significantly reduce the NO in discharge flue gas to the control of technic index
xcontent, belongs to environmentally friendly technology method.
The invention provides a kind of coal carbonization method, its technical scheme is:
(a) from high temperature coal ash and coal dust raw material contact heat transfer in mixing tank of flue gas removing tank, through transfer lime, carry out contact heat transfer reaction and enter dry distillation reactor device proceeding dry distillation reactor, after reaction, generate gas-oil separation and go out reaction generation oil gas and semicoke; Isolated reaction generation oil gas and the oil gas collection chamber of stripped vapor in dry distillation reactor device enter fractionating system and carry out fractionation;
(b) isolated semicoke enters downwards in stripping stage by dry distillation reactor device, through stripping rear section semicoke, enters semicoke blow-down drum discharger; Another part semicoke enters by semicoke inclined tube the device of making charcoal and makes charcoal;
(c) enter the semicoke of the device of making charcoal and contact and make charcoal with main air from the device of making charcoal, the regeneration semicoke of generation with on flue gas, be advanced into tubular type make charcoal device with supplement the wind of making charcoal entering and again contact and make charcoal; High temperature coal ash after making charcoal enters in flue gas removing tank separated with flue gas, and the high temperature coal ash after separation enters mixing tank.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the high temperature coal ash from flue gas removing tank in described step (a) enters mixing tank downwards, with the coal dust raw material contact heat transfer in mixing tank that enters mixing tank through feed-pipe.
A kind of coal carbonization method of the present invention, its further technical characterictic is: in described step (a), after reaction, generate the cyclonic separator of oil gas in dry distillation reactor device and carry out separation, isolate reaction and generate oil gas and semicoke.
A kind of coal carbonization method of the present invention, its further technical characterictic is: in described step (b), isolated semicoke enters downwards in stripping stage by dry distillation reactor device, through water vapor stripping rear section semicoke, after heat collector cooling, enters semicoke blow-down drum discharger; Another part semicoke enters by semicoke inclined tube and semicoke flowrate control valve the device of making charcoal and makes charcoal.
A kind of coal carbonization method of the present invention, its further technical characterictic is: in described step (b), part semicoke passes through semicoke temperature≤80 ℃ of semicoke blow-down drum discharger after heat-obtaining.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the semicoke that enters the device of making charcoal in described step (c) with from the main air of distributor pipe of cardinal wind in the device of making charcoal, contact and make charcoal.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the cyclonic separator that the high temperature coal ash after making charcoal in described step (c) enters in flue gas removing tank is separated with flue gas, the flue gas after separation is discharged flue gas removing tank through flue gas removing tank collection chamber; High temperature coal ash after separation enters mixing tank as thermal barrier downwards by high temperature coal ash transfer lime and high temperature coal ash flowrate control valve.
A kind of coal carbonization method of the present invention, its further technical characterictic is: in described dry distillation reactor device, the coal dust raw material dry distillation reactor time is 2～10min, and dry distillation reactor temperature is 450～560 ℃, and dry distillation reactor absolute pressure is 0.10～0.40MPa.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the fine powder raw material that in described step (a), coal dust raw material is particle diameter≤5mm.
A kind of coal carbonization method of the present invention, its further technical characterictic is: it is to realize in mixing tank and transfer lime that the middle coal dust raw material of described step (a) mixes with high temperature coal ash, high temperature coal ash is 0.1～3.0 with coal dust raw material weight ratio, and it is 450～560 ℃ that mixing temperature is controlled.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the charcoal temperature of described semicoke in the device of making charcoal is 650～760 ℃, and the time of making charcoal is 3～10min, and absolute pressure is 0.1～0.40MPa.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the tubular type device charcoal temperature of making charcoal is 650～760 ℃ in described step (c), and the time of making charcoal is 1～25s.
A kind of coal carbonization method of the present invention, its further technical characterictic is: in described step (c), supplementing the wind of making charcoal entering is fresh air, is preferably pressurized air, and its air linear speed is 2.0～25m/s.This pressurized air meets conventional compressed-air actuated general feature, and its flow can be multiplied by the required air quantity calculating when burning of unit weight charcoal according to total carbon content of circulation semicoke to be determined.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the main purpose of flue gas removing tank is the flue gas of carrying secretly that removes high temperature coal ash, in described step (c), the linear gas velocity of flue gas removing tank is 0.15～0.8m/s, and the reserve of flue gas removing tank high temperature coal ash can be determined according to the residence time 0.5～3min of the required high temperature coal ash internal circulating load of coal dust raw material destructive distillation and high temperature coal ash.
A kind of coal carbonization method of the present invention, its further technical characterictic is: the main air of making charcoal in device in described step (c) is pressurized air, its flow target is to control the temperature of the device high temperature coal ash of making charcoal.This pressurized air meets conventional compressed-air actuated general feature.
The present invention compared with prior art, has following beneficial effect:
1, the semicoke from dry distillation reactor device enters the device of making charcoal, and making charcoal of semicoke completes more than 80% in the device of making charcoal, and controls the air quantity of making charcoal and make to make charcoal in the flue gas of device outlet containing the CO concentration of 1～5v%, so that the NO in reduction flue gas
xfor N
2, reach the NO reducing in regenerated flue gas
xthe object of content.The temperature of making charcoal in device is 650～760 ℃, and air linear speed is 0.2～1.25m/s, and the time of making charcoal is 3～10min, and absolute pressure is 0.1～0.40MPa.
2, adopt the tubular type device technology of making charcoal.The tubular type device of making charcoal is set on the device top of making charcoal, the make charcoal air flow quantity of making charcoal of device bottom of tubular type can be adjusted flexibly, and enter tubular type make charcoal device regeneration semicoke all the time with supplement the oxygen containing fresh air of making charcoal of richness entering and contact, on the one hand strengthened the make charcoal ability of making charcoal of device of tubular type, the tubular type device intensity of making charcoal of making charcoal is increased, improved the efficiency of making charcoal; Can effectively eliminate on the other hand the CO making charcoal in device outlet flue gas, be conducive to environment protection.The tubular type device charcoal temperature of making charcoal is 650～760 ℃, and the tubular type device bottom of making charcoal supplements the fresh air of making charcoal, and its total air linear speed is 2.0～25m/s, and the time of making charcoal is 1～25s.
3, adopt semicoke outer drainage technique continuously, can significantly reduce tubular type make charcoal device and the total load of making charcoal of device of making charcoal, always burn that the decline of wind consumption, plant energy consumption significantly reduce, apparatus structure size reduction makes facility investment decline.The semicoke that discharger has high heating value can be used as circulating fluidized bed boiler fuel or further utilizes as producing synthetic gas synthesizing methanol raw material.
4, flue gas removing tank main purpose is the flue gas of carrying secretly that removes high temperature coal ash, linear gas velocity is 0.15～0.8m/s, and the reserve of flue gas removing tank high temperature coal ash can be determined according to the residence time 0.5～3min of the required high temperature coal ash internal circulating load of coal dust raw material destructive distillation and high temperature coal ash.
5, adopt the coal dust raw material of particle diameter≤5mm, can guarantee raw material normal fluidisation and destructive distillation in device, obtain higher coal tar yield.Under processing condition of the present invention, coal tar productive rate accounts for 85～105% of coal dust oleaginousness (aluminium rice steamer method).In coal chemical technology, by coal raw material crushing, to particle diameter≤5mm, be ripe technically at present.
6, device does not need to adopt dry gas as promoting medium, can make the energy consumption of device further reduce.
In a word, adopt the present invention to have: 1. adopt the device of making charcoal to add the tubular type compound technology of making charcoal of device of making charcoal and improve and make charcoal efficiency and provide enough thermals source for coal dust destructive distillation; 2. outer row's semicoke content is high, calorific value is high; 3. coal dust raw material pyrolysis temperature is stable, and treatment capacity is large, and coal tar productive rate is high; 4. the system of making charcoal that the present invention adopts can significantly reduce the NO in device discharge flue gas
xcontent, is conducive to protection of the environment, has certain social benefit; 5. process make charcoal-high temperature of coal dust raw material device charging-destructive distillation-half afocal row-semicoke coal ash cyclical operation continous-stable, the flexible adjustment of particle diameter≤5mm.The present invention is specially adapted to the destructive distillation processing of various coal dust raw materials.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram of a kind of coal carbonization method of the present invention.
Reference numeral shown in figure is: 1-flue gas; 2-flue gas collection chamber; Cyclonic separator in 3a-flue gas removing tank; Cyclonic separator in 3b-flue gas removing tank; 4-high temperature coal ash transfer lime; The 5-tubular type device of making charcoal; 6-coal dust raw material; 7-coal dust material feeding tube; 8-mixing tank; 9-transfer lime; Cyclonic separator in 10a-dry distillation reactor device; Cyclonic separator in 10b-dry distillation reactor device; The 11-fresh air of making charcoal; 12a-semicoke inclined tube; 12b-semicoke inclined tube; The 13-device of making charcoal; 14-main air; 15-flue gas removing tank; 16-oil gas; 17-high temperature coal ash flowrate control valve; 18-oil gas collection chamber; 19-dry distillation reactor device; 20-stripping stage; 21-stripped vapor; 22-semicoke blow-down drum; 23-heat collector; 24a-semicoke flowrate control valve; 24b-semicoke flowrate control valve; 25-distributor pipe of cardinal wind.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further detailed explanation, and the drawings and specific embodiments do not limit the scope of protection of present invention.
A kind of coal carbonization method of the present invention is as follows as shown in Figure 1:
(a) the high temperature coal ash from flue gas removing tank 15 enters mixing tank 8 downwards, carry out contact heat transfer with the coal dust raw material 6 (particle diameter≤5mm) that enters mixing tank 8 through feed-pipe 7, through transfer lime 9, carry out contact heat transfer reaction and enter dry distillation reactor device 19 proceeding dry distillation reactor, after reaction, generate cyclonic separator 10a, the 10b of oil gas 16 in dry distillation reactor device 19 and carry out separation; Isolate reaction and generate oil gas 16 and semicoke, isolated reaction generation oil gas 16 enters fractionating system with the oil gas collection chamber 18 of stripped vapor in dry distillation reactor device 19 and carries out fractionation.
(b) isolated semicoke enters downwards in stripping stage 20 by dry distillation reactor device 19, through water vapor 21 stripping rear portion semicokes through heat collector 23 heat-obtainings be cooled to≤80 ℃ enter semicoke blow-down drum 22 dischargers; Another part semicoke enters by semicoke inclined tube 12b and semicoke flowrate control valve 24b the device 13 of making charcoal and makes charcoal.Enter the semicoke of the device 13 of making charcoal and contact and make charcoal with main air 14 from the interior distributor pipe of cardinal wind 25 of device 13 of making charcoal, the regeneration semicoke of generation with on flue gas, be advanced into tubular type make charcoal device 5 with supplement the fresh air 11 of making charcoal entering and again contact and make charcoal; High temperature coal ash after making charcoal enters cyclonic separator 3a, 3b in flue gas removing tank 15, and to carry out high temperature coal ash separated with flue gas, and the flue gas 1 after separation is discharged flue gas removing tanks 15 through flue gas removing tank collection chamber 2; High temperature coal ash after separation enters mixing tank 8 as thermal barrier downwards by high temperature coal ash transfer lime 4 and high temperature coal ash flowrate control valve 17 and provides thermal source for 6 destructive distillation of coal ash raw material.
Technical problem to be solved by this invention is to provide a kind of coal carbonization method, the method is produced on coal tar device and has been adopted the device of making charcoal to add the coal dust raw material that tubular type is made charcoal in device heating feed-pipe in the destructive distillation of coal dust (particle diameter≤5mm) raw material, and the high temperature coal ash that the device of making charcoal generates is high containing charcoal semicoke technology as the supplemental heat source of coal dust destructive distillation, outer row.The system of making charcoal of the method consists of make charcoal device and flue gas removing tank of the device of making charcoal, tubular type from the bottom to top successively, by can significantly reduce the NO in discharge flue gas to the control of technic index
xcontent, belongs to environmentally friendly technology method.The present invention has: coal dust (particle diameter≤5mm) charging continuously, fluidized retoring temperature-stable, high temperature coal ash be with low, the outer row's semicoke of coal dust raw material blending ratio content is high, tubular type is made charcoal device and the compound technology of making charcoal of the device of making charcoal is controlled strong to the actuator temperature of making charcoal, the high grade of coal tar productive rate many advantages.
Described semicoke heat collector 23 semicoke is cooled to≤80 ℃ of dischargers.
Described flue gas removing tank 15 main purposes are the flue gases of carrying secretly that remove high temperature coal ash, linear gas velocity is 0.15～0.8m/s, and the reserve of flue gas removing tank 15 high temperature coal ash can be determined according to the residence time 0.5～3min of the required high temperature coal ash internal circulating load of coal dust raw material destructive distillation and high temperature coal ash.
The operational condition of described dry distillation reactor device 19 is: temperature of reaction is 450～560 ℃, preferably 470～550 ℃, is preferably 500～520 ℃; The destructive distillation time is 2～10min, 3.0～7.0min preferably, and being preferably is 4～5min.Coal dust raw material 6 contacts contact heat transfer by mixing tank 8 with high temperature coal ash and enters transfer lime 9, and high temperature coal ash is 0.1～3.0 with coal dust raw material mixed weight ratio, and mixing temperature is 450～560 ℃.High temperature coal ash and coal dust raw material weight are more definite than the heat calculation when mixing; Dry distillation reactor device reaction absolute pressure is 0.10～0.40MPa.
The stripping condition of the stripping stage 20 of described dry distillation reactor device 19 is conventional, and stripping medium is hyperthermia and superheating water vapor, and stripping temperature is 480～520 ℃.
Making charcoal of described semicoke completes more than 80% in the device 13 of making charcoal, and the charcoal temperature in the device 13 of making charcoal is 650～760 ℃, and air linear speed is 0.2～1.25m/s, and the time of making charcoal is 3～10min, and absolute pressure is 0.1～0.40MPa.The main air amount of making charcoal can according to coking yield and semicoke not exclusively the scheme of making charcoal determine.
Supplement the richness enter oxygen containing make charcoal fresh air 11 with enter that tubular type makes charcoal that the regeneration semicoke of device 5 contacts and along the tubular type residue charcoal that the up burning-off of device 5 regenerates on semicoke of making charcoal, and the CO that makes charcoal in device 13 of burning-off.The tubular type device charcoal temperature of making charcoal is 650～760 ℃, and air linear speed is 2.0～25m/s, and the time of making charcoal is 1～25s.
Described make charcoal device and the tubular type compound technology of making charcoal of device of making charcoal has improved the efficiency of making charcoal of device, has reduced the reserve of system, has dwindled equipment size, and plant investment is declined, and can reduce discharge harmful substances from flue gases CO and NO simultaneously
xcontent, be conducive to environment protection.
Described semicoke is outer drainage technique continuously, can significantly reduce tubular type make charcoal device and the total load of making charcoal of device of making charcoal, always burn that the decline of wind consumption, plant energy consumption significantly reduce, apparatus structure size reduction makes facility investment decline.The semicoke that discharger has high heating value can be used as circulating fluidized bed boiler fuel or further utilizes as producing synthetic gas synthesizing methanol raw material.
Described coal dust raw material particle size≤5mm, oleaginousness (aluminium Zhen method) 5～35%.In coal chemical technology, by coal raw material crushing, to particle diameter≤5mm, be ripe technically at present.
The technician of coal chemical technology is clearly to the operation of the dry distillation of coal and control process, can select aforesaid operations condition according to concrete operations situation.
Comparative example
Adopt Yima coal powder raw material, feedstock property is in Table 1, and the operational condition of destructive distillation condition, product distribute in Table 2.
Embodiment 1
Adopt Yima coal powder raw material, feedstock property is in Table 3.
Coal dust destructive distillation is carried out on the fluidizer of laboratory, and semicoke adopts to make charcoal and after device is made charcoal, enters tubular type and make charcoal in device and make charcoal, and semicoke enters the device of making charcoal and controls by main air amount the actuator temperature of making charcoal.Semicoke is made charcoal after device is made charcoal and is entered flue gas removing tank through make charcoal device and tubular type.The stripping medium of dry distillation reactor device stripping stage is water vapor, and stripping temperature is 500 ℃.The operational condition of the present embodiment coal dust destructive distillation device, product distribution and portioned product character are in Table 4.
Embodiment 2
Press embodiment 1, difference is that weight ratio, dry distillation reactor device pyrolysis temperature, dry distillation reactor device destructive distillation time, the tubular type of flue gas removing tank linear speed, the actuator temperature of making charcoal, the device time of making charcoal, coal dust raw material and high temperature coal ash actuator temperature, the tubular type device of making charcoal of making charcoal burns time, the tubular type device linear speed of making charcoal.The operational condition of the present embodiment coal dust destructive distillation device, product distribution and portioned product character are in Table 5.
Embodiment 3
Press embodiment 1, difference is that weight ratio, dry distillation reactor device pyrolysis temperature, dry distillation reactor device destructive distillation time, the tubular type of flue gas removing tank linear speed, the actuator temperature of making charcoal, the device time of making charcoal, coal dust raw material and high temperature coal ash actuator temperature, the tubular type device of making charcoal of making charcoal burns time, the tubular type device linear speed of making charcoal.The operational condition of the present embodiment coal dust destructive distillation device, product distribution and portioned product character are in Table 6.
Embodiment 4
Press embodiment 1, difference is that weight ratio, dry distillation reactor device pyrolysis temperature, dry distillation reactor device destructive distillation time, the tubular type of flue gas removing tank linear speed, the actuator temperature of making charcoal, the device time of making charcoal, coal dust raw material and high temperature coal ash actuator temperature, the tubular type device of making charcoal of making charcoal burns time, the tubular type device linear speed of making charcoal.The operational condition of the present embodiment coal dust destructive distillation device, product distribution and portioned product character are in Table 7.
Table 1 comparative example coal dust feedstock property
The operational condition of table 2 comparative example fixed bed coal dried bean noodles distillation unit, product distribute and portioned product character
Table 3 coal dust feedstock property (embodiment 1)
The operational condition of table 4 embodiment 1 coal dust destructive distillation device, product distribute and portioned product character
The operational condition of table 5 embodiment 2 coal dust destructive distillation devices, product distribute and portioned product character
The operational condition of table 6 embodiment 3 coal dust destructive distillation devices, product distribute and portioned product character
The operational condition of table 7 embodiment 4 coal dust destructive distillation devices, product distribute and portioned product character
Claims (13)
1. a coal carbonization method, is characterized in that comprising the steps:
(a) from high temperature coal ash and coal dust raw material contact heat transfer in mixing tank of flue gas removing tank, through transfer lime, carry out contact heat transfer reaction and enter dry distillation reactor device proceeding dry distillation reactor, after reaction, generate gas-oil separation and go out reaction generation oil gas and semicoke; Isolated reaction generation oil gas and the oil gas collection chamber of stripped vapor in dry distillation reactor device enter fractionating system and carry out fractionation;
(b) isolated semicoke enters downwards in stripping stage by dry distillation reactor device, through stripping rear section semicoke, enters semicoke blow-down drum discharger; Another part semicoke enters by semicoke inclined tube the device of making charcoal and makes charcoal;
(c) enter the semicoke of the device of making charcoal and contact and make charcoal with main air from the device of making charcoal, the regeneration semicoke of generation with on flue gas, be advanced into tubular type make charcoal device with supplement the wind of making charcoal entering and again contact and make charcoal; High temperature coal ash after making charcoal enters in flue gas removing tank separated with flue gas, and the high temperature coal ash after separation enters mixing tank.
2. coal carbonization method according to claim 1, is characterized in that: the high temperature coal ash from flue gas removing tank in described step (a) enters mixing tank downwards, with the coal dust raw material contact heat transfer in mixing tank that enters mixing tank through feed-pipe.
3. coal carbonization method according to claim 1, is characterized in that: in described step (a), after reaction, generate the cyclonic separator of oil gas in dry distillation reactor device and carry out separation, isolate reaction and generate oil gas and semicoke.
4. coal carbonization method according to claim 1, is characterized in that: the fine powder raw material that described step (a) coal dust raw material is particle diameter≤5mm.
5. coal carbonization method according to claim 1, it is characterized in that: isolated semicoke enters downwards in stripping stage by dry distillation reactor device in described step (b), through water vapor stripping rear section semicoke, after heat collector cooling, enter semicoke blow-down drum discharger; Another part semicoke enters by semicoke inclined tube and semicoke flowrate control valve the device of making charcoal and makes charcoal.
6. coal carbonization method according to claim 4, is characterized in that: in described step (b), part semicoke passes through semicoke temperature≤80 ℃ of semicoke blow-down drum discharger after heat-obtaining.
7. coal carbonization method according to claim 1, is characterized in that: in described step (c), enter the semicoke of the device of making charcoal with from the device of making charcoal in the main air of distributor pipe of cardinal wind contact and make charcoal.
8. coal carbonization method according to claim 1, it is characterized in that: the cyclonic separator that the high temperature coal ash after making charcoal in described step (c) enters in flue gas removing tank is separated with flue gas, the flue gas after separation is discharged flue gas removing tank through flue gas removing tank collection chamber; High temperature coal ash after separation enters mixing tank as thermal barrier downwards by high temperature coal ash transfer lime and high temperature coal ash flowrate control valve.
9. coal carbonization method according to claim 1, is characterized in that: in described dry distillation reactor device, the coal dust raw material dry distillation reactor time is 2～10min, and dry distillation reactor temperature is 450～560 ℃, and dry distillation reactor absolute pressure is 0.10～0.40MPa.
10. coal carbonization method according to claim 1, is characterized in that: in described step (a), high temperature coal ash is 0.1～3.0 with coal dust raw material weight ratio, and it is 450～560 ℃ that mixing temperature is controlled.
11. coal carbonization methods according to claim 1, is characterized in that: the charcoal temperature of described semicoke in the device of making charcoal is 650～760 ℃, and the time of making charcoal is 3～10min, and absolute pressure is 0.1～0.40MPa.
12. coal carbonization methods according to claim 1, is characterized in that: the tubular type device charcoal temperature of making charcoal is 650～760 ℃ in described step (c), and the time of making charcoal is 1～25s.
13. coal carbonization methods according to claim 1, is characterized in that: in described step (c), supplementing the wind of making charcoal entering is pressurized air, and air linear speed is 2.0～25m/s.
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| 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 |
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