CN102911686B - Coal destructive distillation method and apparatus - Google Patents
Coal destructive distillation method and apparatus Download PDFInfo
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- CN102911686B CN102911686B CN201110219229.0A CN201110219229A CN102911686B CN 102911686 B CN102911686 B CN 102911686B CN 201110219229 A CN201110219229 A CN 201110219229A CN 102911686 B CN102911686 B CN 102911686B
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Abstract
The invention discloses a coal destructive distillation method and a coal destructive distillation apparatus. The method and apparatus are characterized in that: a coal powder raw material is arranged in a tubular charcoal burning device and is arranged coaxially therewith; the charcoal burning device is arranged on the upper part of a destructive distillation reactor; high-temperature coal ash from the charcoal burning device is delivered downwards and enters a high-temperature coal ash delivery pipe; in the high-temperature coal ash delivery pipe, the high-temperature coal ash is mixed with the coal powder raw material (with a particle size no larger than 3mm) entering the destructive distillation reactor from a feeding pipe, and is subjected to heat transfer; the mixture enters the destructive distillation reactor and is subjected to a destructive distillation reaction; oil gas generated by the reaction is subjected to separation and stripping; separated and stripped oil gas is subjected to fractionation; part of the semi-coke obtained after separation and stripping is subjected to heat extraction and is discharged from the apparatus; and another part of the semi-coke enters the tubular charcoal burning device and is subjected to charcoal burning, such that regenerated semi-coke is obtained; the regenerated semi-coke enters the charcoal burning device and further charcoal burning is carried out; produced high-temperature coal ash is recycled as a supplementary heat source of destructive distillation of the coal ash raw material in the destructive distillation reactor. The method and the apparatus provided by the invention is especially suitable for destructive distillation processing of various coal powder raw materials, and has the advantages of continuous and stable operation, flexible adjustment, and the like.
Description
Technical field
The invention belongs to coal chemical technology, relate to a kind of coal carbonization method and device.
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 is taking 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 DEG C, the moisture in coal evaporates; When temperature is elevated to more than 200 DEG C, in coal, disengage in conjunction with water; When more than 350 DEG C, caking coal starts to soften, and further forms the plastic mass (this phenomenon does not occur for mud coal, brown coal etc.) of thickness; Separate out to 400～500 DEG C of most of dry gas and tar, claim one time thermal decomposition product; At 450～550 DEG C, thermolysis is proceeded, residue retrogradation solidify to form semicoke gradually; Higher than 550 DEG C, 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 DEG C, and the hardening of semicoke volume-diminished forms porous coke.In the time that 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 raw material ature of coal, processing conditions (being mainly 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, be artificial petroleum important sources it
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.
By Lu Qi Rule Gas Company method (Lurgi Ruhrgas) of Lurgi GmbH company (Germany) and Ruhrgas AG company (U.S.) development research (Guo Shucai chief editor. Coal Chemical Industry technology (second edition). Beijing: Chemical Industry Press, 2006,22-24.), 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 part of circulation is left upright furnace pneumatic conveyor and promoted heating, after separating, turns back to upright furnace as thermal barrier with waste gas 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 (Guo Shucai of Dalian University of Technology's exploitation, Luo Changqi, Zhang Daijia etc., brown coal solid thermal carriers destructive distillation new technology type approval test. Journal of Dalian University of Technology Total, 1995,35 (1): 46-50.), 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.Destructive distillation produce semicoke be thermal barrier, be 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 heat is passed to raw material particle by the semicoke of high temperature, and rate of heating is very fast, and coal Rapid Thermal occurs and decomposes.Because the volatile matter that the pyrolysis of coal grain produces is drawn very soon, secondary pyrolysis is lighter, therefore new distillation process coal tar productive rate is higher.The material mixing through mixing tank enters reactive tank, completes retort process at this, separates out destructive distillation gaseous product, i.e. volatility product.Reactive tank solid product semicoke enters burner through material feeder.The air of semicoke or the fuel adding and preheating burns, and makes semicoke reach the temperature that thermal barrier specifies, is thus lifted to primary cyclone in riser tube, and semicoke separates with flue gas.Hot semicoke, from primary cyclone people aggregate groove, circulates as thermal barrier.Unnecessary semicoke is sent outside as destructive distillation product through discharge groove.Flue gas after secondary cyclone dedusting outside row.After destructive distillation gaseous product autoreaction groove is derived, separate out tar and water through fly-ash separator, air cooler and water cooler.Coal gas drying is sloughed moisture, under-30 DEG C of left and right conditions, carry out freezing, the gasoline in gas recovery.Purified gas is sent after vacuum fan and metering.
By U.S. FMC and OCR develop jointly COED technology (Zeng Erxun. be translated from " Fuel Processiong Technology " Vol4.No.2+3,1981.), the raw material that this process using low pressure, multistage, fluidized bed coal distillation process mean particle size are 0.2mm, order is by the reactor of four series connection, wherein first step reactor plays the dry and preheating of coal, in the end in A reactor, the semicoke producing is carried out to partial gasification with the mixture of water vapour and oxygen in intermediate reactor.The coal gas that gasification produces is as thermal barrier and the fluidizing medium of pyrolysis reactor and moisture eliminator.Flow by means of solid phase and gas-phase reverse stream, make reaction zone improve temperature according to the requirement of coal degassing degree, effectively control the carrying out of pyrolytic process.Pyrolysis is carried out under pressure 35～70kPa.The finished product are semicoke, middle calorific value (15～18MJ/m
3) coal gas and coal-based crude oil, the latter obtains with pyrolysis liquid product catalysis under pressure 17～21MPa (Ni-Mo) Hydrogenation.
The O of CSIR of Australia in 20 century 70s begin one's study mid-term with the method for quick coal pyrolyzing (Wu Yongkuan. the exploitation situation of external coal low-temperature pyrolysis technology and the problem facing. ature of coal technology (COAL QUALTYEND TECHNOLOGY), 1995,1:43-44.) to obtain liquid fuel, 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 (< 0.2mm) of pulverizing is sprayed in the sand bed of reactor with nitrogen, and rate of heating is about 104 DEG C/s, and the main process of pyrolytic reaction completes in 1s.In addition pyrolytic tar is also carried out to structural analysis, and carried out the research of hydrogenation of tar processing with several dissimilar reactors.
The research and development of Occidental Research Co. (US) 10889 Wilshire Blvd, Los Angeles, California 90024, of the Garrett Fa Shi U.S. (Wu Yongkuan. the exploitation situation of external coal low-temperature pyrolysis technology and the problem facing. ature of coal technology (COAL QUALTYEND TECHNOLOGY), 1995,1:39-40.).To be crushed to the coal dust of 0.1mm, in normal pressure entrained-flow reactor, carry out pyrolysis.This technique is the be used as power fuel design of boiler of production fluid body and geseous fuel and being suitable for of making a living, and it is according to being that the quick destructive distillation of short residence time(SRT) can obtain higher tar yield.Thermal barrier is the self-produced circulation semicoke of using through air heating.Pyrolysis occurred in part second, and the residence time is less than 2s, thereby volatile matter second pyrolysis minimum, and liquid yield is high.At 577 DEG C, tar yield is up to 35 quality %.In entrained-flow reactor, fluidizing medium is the coal gas utilizing after charing, after isolating pyrolysis char and liquid product, turns back in the recycle system.Liquid product carries out Hydrogenation and becomes coal-based crude oil.Obtain in addition semicoke and thermal value 22～24MJ/m
3middle calorific value of gas.
Holder scott (Toscoal) method be Oil Shale Corporation of America (Oil Sha lecorp) and the exploitation of Rocky Flats research centre (Guo Shucai edits. Coal Chemical Industry technology (second edition). Beijing: Chemical Industry Press, 2006,19-20.).Coal previously prepared and preheating is sent in rotary kiln, contacts and pyrolysis occurs at this with fervid porcelain ball thermal barrier.Pyrolysis product causes gas sweetening and hydrocarbon polymer recovery system.After porcelain ball separates in mechanical separator with semicoke, with the heat direct heating of a part of self-produced dry distillation gas-fired, then return in rotary kiln as solid circle thermal barrier.Waste gas after heating porcelain ball is for the preheating of coal.The product of technique is that semicoke, oil and calorific value are 22MJ/m
3coal gas.
The coal Rapid Thermal solution of Japan (Xu Zhengang, the Development of Coal Flash Pyrolysis Process of Japan. clean coal technology, 2001,7 (1): 48-51,56.), the method is the pyrolytic technique showing unique characteristics that coal gasification and pyrolysis are combined.It can obtain to greatest extent gaseous state (coal gas) and liquid state (tar and benzene class) product from high volatile feed coal.Feed coal drying, and be milled down to 80% and be less than after 0.074mm, the gas that produces with nitrogen or pyrolysis is close to be carried mutually, sprays into the pyrolysis section of reactor through feeder.Then by the high-temperature gas rapid heating producing from hypomere carbonization at low temperature, under 600～950 DEG C and 0.3MPa, fast pyrogenation in several seconds, produces gaseous state and liquid product and solid semicoke.In pyrolysis section, gaseous state and solid product upwards flow simultaneously.Solid semicoke is through high temperature cyclone separator after separating gas, and the gasification section of a part of Returning reactor and oxygen and water vapour generating gasification under 1500～1650 DEG C and 0.3MPa is reacted, and provides thermal source for the pyrolytic reaction of epimere; All the other semicokes are after interchanger recovery waste heat, as solid semicoke product.From high temperature cyclone separator high-temperature gas out, contain gaseous state and liquid product, through an indirect type interchanger recovery waste heat, and then after de-benzene, desulfurization, deamination and other purifying treatment, as gaseous product.Indirect type interchanger adopts oil as heat transferring medium, and the waste heat reclaiming from coal gas is used for producing steam.The benzene class producing in the tar producing in coal gas process of cooling and scavenging process is as main liquid product.
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.
A kind of fluid bed powder coal low-temperature pyrolysis multi-joint-production apparatus that China Patent Publication No. CN 201395576 is related, comprises fine coal destructive distillation unit, gasification unit and fuel element.Fine coal destructive distillation unit, gasification unit and fuel element can also can move simultaneously in isolated operation, or fine coal destructive distillation unit and gasification unit and fuel element combined running.Fine coal destructive distillation unit melts poly-fine coal gas retort, one-level tornado dust collector, second cyclone dust extractor, pyrolysis gas cooling and purifying system, blower system, pyrolysis gas storage tank, semicoke bucket and semicoke delivery system by ash and forms; Gasification unit is melted poly-powder coal gasification furnace, high-temperature dust removal system, Waste Heat Recovery System (WHRS), middle temperature dust-removal system and gas washing cooling tower by ash and is formed.It is convenient that this device operation is controlled.Feed coal strong adaptability, stable operation, immunity from interference is strong, turndown ratio large (70～120%), device is easy to realize long-period stable operation, safety and environmental protection.But this technique fuel element does not relate to the tubular type device technology of making charcoal of making charcoal, and there is following some deficiency in this Technology: one, ash melts poly-fine coal destructive distillation by strengthening the quantity combusted that generates semicoke, so that the enough coal ash of output meet the required thermal barrier of fine coal destructive distillation and thermal source; Two, the quantity combusted conference of generation semicoke makes the equipment size of fuel element large, causes plant investment to increase; Three, owing to adopting ash to melt poly-fine coal destructive distillation, to produce ash oontent in semicoke high.
The related a kind of piston type fluidized bed low temperature dry distillation technological process of coal dust of China Patent Publication No. CN 101328415 utilizes lifting tube flowing catalytic cracking device principle, taking the riser reactor of lifting tube flowing catalytic cracking device as dry distillation reactor device, taking the catalyst regenerator of lifting tube flowing catalytic cracking device as high-temperature water gas producer, fluidizing medium and thermal barrier taking high-temperature water gas as 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, after reaction, oil gas separates 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 DEG C～550 DEG C of operating temperatures, move approximately 4 hours, and Heating Zone Temperature regulates and controls between 700～800 DEG C, 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 control is lower, tar yield is improved, below 50%, bring up to present more than 80% by the former rate of recovery.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.
Summary of the invention
The object of this invention is to provide a kind of coal carbonization method and device, with solve existing coal dust destructive distillation device exist the device of making charcoal to make charcoal the large and temperature of load cannot flexible and the problem such as control, high temperature coal ash and high, the outer row's semicoke of coal dust raw material blending ratio content are low and energy consumption is high.Use the present invention can significantly reduce tubular type make charcoal device and the total load of making charcoal of device of making charcoal, always burn that wind consumption declines, plant energy consumption significantly reduces, apparatus structure size reduction makes facility investment decline, the semicoke that discharger has a high heating value in addition also can be used as circulating fluidized bed boiler fuel or further utilizes as producing synthetic gas synthesizing methanol raw material, has saved the energy.
The invention provides a kind of coal carbonization method, it is characterized in that comprising the steps:
I) the coal dust raw material of particle diameter≤3mm is arranged on after the feed-pipe that tubular type makes charcoal in device promoting to enter under the effect of gas, be mixed into dry distillation reactor device with the high temperature coal ash from the device of making charcoal and carry out destructive distillation, reaction generates the I cyclonic separator of oil gas in dry distillation reactor device and separates, isolated reaction generation oil gas enters fractionating system and carries out fractionation, and isolated semicoke enters Step II);
II) from step I) semicoke the semicoke dense bed and the stripping stage that enter in dry distillation reactor device carry out stripping, after stripping, part semicoke is discharger after heat-obtaining cooling, another part semicoke enters tubular type and makes charcoal that device bottom contacts with the wind of making charcoal and make charcoal along tubular type that device is up makes charcoal, the separating of regenerate afterwards semicoke and flue gas;
III) the regeneration semicoke after separation enters in the high temperature coal ash dense bed of the device of making charcoal, charcoal on burning-off regeneration semicoke, the high temperature coal ash that the device of making charcoal generates after making charcoal is mixed into dry distillation reactor device as thermal barrier by high temperature coal ash transfer lime and the coal dust raw material of making charcoal after device heating through tubular type, the tubular type flue gas discharger generating after device and the device of making charcoal are made charcoal of making charcoal.
The inventive method is further characterized in that: described a part of semicoke after stripping through heat-obtaining be cooled to≤80 DEG C after discharger.
The inventive method is further characterized in that: described a part of semicoke after stripping through heat collector heat-obtaining be cooled to≤80 DEG C enter semicoke blow-down drum discharger.
The inventive method is further characterized in that: described another part semicoke after stripping enters the tubular type device bottom of making charcoal by I semicoke inclined tube and I semicoke flowrate control valve.
The inventive method is further 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 460～560 DEG C, and dry distillation reactor absolute pressure is 0.10～0.40MPa.
The inventive method is further characterized in that: water-content≤15 % by weight in described coal dust raw material.
The inventive method is further characterized in that: coal dust raw material carried out with mixing in high temperature coal ash transfer lime of high temperature coal ash, and high temperature coal ash is 0.01～1.5 with coal dust raw material weight ratio, and mixing temperature is 460～560 DEG C.
The inventive method is further characterized in that: described lifting gas adopts dry gas or water vapor.
The inventive method is further characterized in that: the linear gas velocity of the lifting gas in feed-pipe is 1.0～15.0m/s, and coal dust raw material is the residence time 1.0～5.0min in feed-pipe, and it is between 450～560 DEG C that coal dust raw material enters the front temperature control of high temperature coal ash transfer lime.
The inventive method is further characterized in that: described another part semicoke after stripping enters tubular type and makes charcoal and contact with the wind of making charcoal behind device bottom and make charcoal along tubular type that device is up makes charcoal, and supplements the wind of making charcoal and enters in the tubular type device middle and upper part of making charcoal.
The inventive method is further characterized in that: tubular type is made charcoal the interior temperature of device between 650～750 DEG C, and the linear speed that the wind of making charcoal is made charcoal in device in tubular type is 1.0～20.0m/s, and the time of making charcoal is 3～40s.
The inventive method is further characterized in that: described in the wind of making charcoal be pressurized air.
The inventive method is further characterized in that: the high temperature coal ash dense bed temperature of making charcoal in device is at 650～750 DEG C, and the operating linear velocity of making charcoal in device is 0～1.2m/s, and the time of making charcoal is 0～5min, and absolute pressure is 0.1～0.40MPa.
The inventive method is further characterized in that: the regeneration semicoke after described separation enters in the high temperature coal ash dense bed of the device of making charcoal, and with the charcoal on main air burning-off regeneration semicoke, main air is pressurized air.
The present invention also provides a kind of coal carbonization device, it is characterized in that: this device comprises the device of making charcoal, the tubular type device of making charcoal, feed-pipe and dry distillation reactor device, dry distillation reactor device comprises I cyclonic separator and stripping stage, the device of making charcoal is connected with dry distillation reactor device by high temperature coal ash transfer lime, it is inner and coaxially arrange with it that feed-pipe is positioned at the tubular type device of making charcoal, feed-pipe outlet is connected with high temperature coal ash transfer lime, feed-pipe import is arranged on make charcoal device bottom of tubular type, the tubular type device top of making charcoal is connected with the device of making charcoal, bottom is connected with the stripping stage of dry distillation reactor device bottom by I semicoke inclined tube.
Apparatus of the present invention are further characterized in that: described coal carbonization device also comprises heat collector, are arranged at dry distillation reactor device outside, are connected with the stripping stage of dry distillation reactor device bottom by II semicoke inclined tube and setting II semicoke flowrate control valve thereon.
Apparatus of the present invention are further characterized in that: described in make charcoal device by high temperature coal ash transfer lime and high temperature coal ash flowrate control valve be thereon set and be connected with dry distillation reactor device.
Apparatus of the present invention are further characterized in that: make charcoal device bottom of described tubular type is connected with the stripping stage of dry distillation reactor device bottom by I semicoke inclined tube and the I semicoke flowrate control valve that arranges thereon.
Apparatus of the present invention are further characterized in that: the described tubular type device of making charcoal is provided with two wind distribution rings of making charcoal, and one is arranged at bottom, and below I semicoke inclined tube entrance; Another is arranged at middle and upper part, and above feed-pipe outlet.
Apparatus of the present invention are further characterized in that: described heat collector and semicoke blow-down drum are connected.
Apparatus of the present invention are further characterized in that: it is characterized in that: described in the device of making charcoal be arranged on dry distillation reactor device top.
Apparatus of the present invention are further characterized in that: described in the make charcoal metal shell liner insulating and wearing-resistant lining of device.
Apparatus of the present invention are further characterized in that: it is circular metal tube that described high temperature coal ash transfer lime adopts cross section, diameter of phi 200～3000mm, entrance is arranged on the top of the device high temperature coal ash dense bed of making charcoal, and outlet position is located at the top at the semicoke dense bed interface in dry distillation reactor device.
Apparatus of the present invention are further characterized in that: described dry distillation reactor device is metal shell liner insulating and wearing-resistant lining.
Apparatus of the present invention are further characterized in that: it is circular metal tube that described feed-pipe adopts cross section, diameter of phi 200～3000mm, and pipeline wall thickness 3～10cm, length is 8～35m.
Apparatus of the present invention are further characterized in that: described feed-pipe is arbitrarily angled connection with high temperature coal ash transfer lime.
Apparatus of the present invention are further characterized in that: tubular type make charcoal device adopt cross section be circular metal tube, liner insulating and wearing-resistant lining, length is 10～40m, diameter of phi 400～5000mm.
Apparatus of the present invention are further characterized in that: the tubular type device of making charcoal is 2.5～20.0 with the diameter ratio of feed-pipe.
The present invention is applicable to the fine powder destructive distillation processing of various coals.
The present invention compared with prior art, has following beneficial effect:
1) the present invention adopts coal carbonization to generate continuously outer row of semicoke, can significantly reduce tubular type make charcoal device and the total load of making charcoal of device of making charcoal, always burn that wind consumption declines, plant energy consumption significantly reduces, 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.
2) the present invention adopts make charcoal device and compound the making charcoal of the device of making charcoal of tubular type can effectively control high temperature shale ashes temperature between 650～750 DEG C, and the present invention's actuator temperature of making charcoal is controlled strong, and overtemperature, assurance device long-term operation are not produced can to protect equipment.In addition, make charcoal device and conventional bed of tubular type made charcoal and had the stronger ability of making charcoal and turndown ratio more flexibly compared with device, make charcoal in device in tubular type, semicoke contacts with fresh air all the time, increase the make charcoal speed of making charcoal of device of tubular type, improved the make charcoal efficiency of making charcoal of device of tubular type, also can reduce thus the regeneration semicoke reserve of the device of making charcoal, dwindle the size of the device of making charcoal, appliance arrangement investment is declined.
3) coal dust heating raw materials of the present invention is mainly realized in tubular type is made charcoal device and in high temperature coal ash transfer lime and high temperature coal ash contact heat transfer, thereby can reduce high temperature coal ash and coal dust raw material blending ratio, thereby improve the carbon content of outer row's semicoke, improve the further utility value of semicoke.
4) the present invention adopts the coal dust raw material of particle diameter≤3mm, can ensure raw material normal fluidisation and destructive distillation in device, obtains 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).
5) coal dust raw material pyrolysis temperature of the present invention is stable, and coal tar productive rate is high, and coal dust feed throughput is large.
6) cyclical operation continous-stable of the present invention, device flexible adjustment.
7) apparatus of the present invention scantlings of the structure declines, and facility investment is low.
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, but do not limit the scope of protection of present invention.
Accompanying drawing and brief description of the drawings
Figure is the schematic diagram of a kind of coal carbonization device of the present invention.
Reference numeral shown in figure is:
The 1-device of making charcoal; The 2-tubular type device of making charcoal; 3-high temperature coal ash transfer lime; 4-high temperature coal ash flowrate control valve; 5-oil gas collection chamber; 6-I cyclonic separator; The 7-I wind distribution rings of making charcoal; 8-dry distillation reactor device; 9-semicoke dense bed; 10-feed-pipe; 11-I semicoke inclined tube; 12-I semicoke flowrate control valve; The 13-II wind distribution rings of making charcoal; 14-coal dust raw material; 15-promotes gas; 16-stripped vapor; 17-semicoke blow-down drum; 18-heat collector; 19-II semicoke flowrate control valve; 20-II semicoke inclined tube; 21-stripping stage; 22-oil gas; 23-main air; 24-distributor pipe of cardinal wind; 25-II cyclonic separator; 26-flue gas collection chamber; 27-flue gas.
Embodiment
As shown be the schematic diagram of a kind of coal carbonization device of the present invention.
This device parts such as device 2, coal dust material feeding tube 10, dry distillation reactor device 8, semicoke heat collector 18, semicoke blow-down drum 17 of mainly being made charcoal by the device 1 of making charcoal, tubular type form.Dry distillation reactor device 8 comprises I cyclonic separator 6, oil gas collection chamber 5, stripping stage 21; The device 1 of making charcoal comprises distributor pipe of cardinal wind 24, II cyclonic separator 25, flue gas collection chamber 26; The tubular type device 2 of making charcoal is provided with two main air distribution rings.The device 1 of making charcoal is connected with dry distillation reactor device 8 by high temperature coal ash transfer lime 3, and it is inner and coaxially arrange with it that coal dust material feeding tube 10 is positioned at make charcoal device 2 of tubular type, and 10 outlets of coal dust material feeding tube are connected with high temperature coal ash transfer lime 3.Make charcoal, between device 1 and dry distillation reactor device 8, high temperature coal ash flowrate control valve 4 is set, the bottom of dry distillation reactor device 8 is provided with stripping stage 21.Stripping stage 21 is connected with I semicoke inclined tube 11 and the II semicoke inclined tube 20 of below respectively.I semicoke inclined tube 11 and II semicoke inclined tube 20 middle parts arrange respectively I semicoke flowrate control valve 12 and II semicoke flowrate control valve 19; Stripping stage 21 bottoms, wherein a road II semicoke inclined tube 20 is connected with heat collector 18, semicoke blow-down drum 17, and semicoke discharge control valve can be set between heat collector 18 and semicoke blow-down drum 17; Another Lu Jing I semicoke inclined tube 11 of stripping stage 21 bottoms and tubular type device 2 bottoms of making charcoal are connected, and tubular type device 2 outlets of making charcoal are connected with the device 1 of making charcoal.
The scantlings of the structure of the described device 1 of making charcoal is determined and is comprised that arranging of cyclonic separator all meets the general feature of the lifting tubular type For Fcc Regenerator of petrochemical industry.It is circular metal tube liner insulating and wearing-resistant lining that the pipeline of high temperature coal ash transfer lime 3 adopts cross section, internal diameter is Φ 200～2000mm, its concrete device diameters determines according to operating air linear speed, and device height is according to semicoke internal circulating load, coal ash reserve and the coal ash of time, the coal ash settling height calculative determination when the sedimentation of making charcoal.
Described high temperature coal ash flowrate control valve 4 is located at makes charcoal on the high temperature coal ash transfer lime 3 being connected between device 1 and dry distillation reactor device 8, can adopt various conventional flowrate control valves (as adopted guiding valve), to regulate the flow of high temperature coal ash, realize the temperature of reaction control to dry distillation reactor device 8.
Described high temperature coal ash transfer lime 3 entrances are arranged on the device 1 high temperature coal ash dense bed top of making charcoal, the below at high temperature coal ash dense bed interface.3 outlets of high temperature coal ash transfer lime are arranged on the top, interface of the inside semicoke dense bed 9 of dry distillation reactor device 8.High temperature coal ash transfer lime 3 diameters are determined according to high temperature coal ash internal circulating load and coal dust inlet amount and the 3 delivery medium density calculations of high temperature coal ash transfer lime.
Described dry distillation reactor device 8 comprises I cyclonic separator 6 and stripping stage 21, its device diameters is determined according to operating air linear speed, height of dense phase is determined according to the residence Time Calculation of resinous shale raw material, dilute phase height is according to the settling height calculative determination of particle semicoke, and stripping stage 21 diameters and height are according to the semicoke charge density calculative determination of semicoke stripping time and stripping stage.
Described tubular type is made charcoal, and to adopt cross section be circular metal tube to device 2, liner insulating and wearing-resistant lining, and length is 10～40m, Φ 400～5000mm; Tubular type make charcoal device 2 concrete diameter according to tubular type make charcoal device 2 operating linear velocity determine, tubular type make charcoal device 2 length according to make charcoal device 1 and dry distillation reactor device 8 total height determine.
Described coal dust material feeding tube 10 entrances are positioned at make charcoal device 2 bottoms by tubular type device 2 inside of making charcoal of tubular type, coaxially arrange with the tubular type device 2 of making charcoal; Material feeding tube 10 setting vertical with high temperature coal ash transfer lime 3, also can arbitrarily angledly arrange, and feed-pipe 10 arranges in the same way and coaxially with high temperature coal ash transfer lime 3 interior Flow of Goods and Materials.It is circular metal tube that coal dust material feeding tube 10 adopts cross section, Φ 200～3000mm, and pipeline wall thickness 3～10cm, feed-pipe 10 height 8～35m, its concrete height is highly determined according to device.
The described tubular type device 2 of making charcoal is 2.5～20.0 with the diameter ratio of feed-pipe 10.
It is circular metal tube liner insulating and wearing-resistant lining that described I semicoke inclined tube 11 and the pipeline of II semicoke inclined tube 20 all adopt cross section, and internal diameter is Φ 300～2000mm, and its diameter is according to semicoke internal circulating load and semicoke operational densities calculative determination wherein.I semicoke flowrate control valve 12 and II semicoke flowrate control valve 19 are located at dry distillation reactor device 8 stripping stages 21 and tubular type and make charcoal on the I semicoke inclined tube 11 and II semicoke inclined tube 20 that device 2 is connected with heat collector 18, can adopt various conventional flowrate control valves (as adopted guiding valve), to regulate semicoke flow.
Described heat collector 18 scantlings of the structure can be carried out calculative determination according to eliminating semicoke flow and heat-obtaining load.It is circular metal vessel that semicoke blow-down drum 17 adopts cross section, meets the general feature of metal vessel.
A kind of coal carbonization method of the present invention is as follows as shown in drawings:
(a) (particle diameter≤3mm) coal dust raw material 14 after pulverizing enters and is arranged on the feed-pipe 10 that tubular type is made charcoal in device promoting under the effect of gas 15, then through high temperature coal ash transfer lime 3 with high temperature coal ash mixing transmission of heat by contact from the device 1 of making charcoal and enter dry distillation reactor device 8 and carry out destructive distillation; After coal dust raw material 14 dry distillation reactors finish, reaction generates the I cyclonic separator 6 of oil gas 22 in dry distillation reactor device 8 and separates, and isolates reaction and generates oil gas 22 and semicoke; Isolated reaction generation oil gas 22 enters fractionating system with the oil gas collection chamber 5 of stripped vapor in dry distillation reactor device 8 and carries out fractionation.
(b) isolated semicoke enters by the dipleg of I cyclonic separator 6 in dry distillation reactor device 8 in the semicoke dense bed 9 and stripping stage 21 of dry distillation reactor device 8, through stripped vapor 16 stripping rear portion semicokes through heat collector 18 heat-obtainings be cooled to≤80 DEG C enter semicoke blow-down drum 17 dischargers; Another part semicoke enters by I semicoke inclined tube 11 and I semicoke flowrate control valve 12 that tubular type makes charcoal that device 2 bottoms and make charcoal from II wind distribution rings 13 and I make charcoal that the wind of making charcoal of wind distribution rings 7 contacts and makes charcoal along tubular type that device 2 is up to carry out relay and make charcoal; Regeneration semicoke after the device 2 of making charcoal by tubular type is made charcoal enters the II cyclonic separator 25 of making charcoal in device 1 semicoke of regenerating and separates with flue gas 27.
(c) the regeneration semicoke after separation enters in the high temperature coal ash dense bed of the device 1 of making charcoal through the dipleg of II cyclonic separator 25, and main air 23 enters the device 1 of making charcoal bottom by distributor pipe of cardinal wind 24 contacts the charcoal on burning-off regeneration semicoke with regeneration semicoke; The coal dust raw material that the high temperature coal ash that the device 1 of making charcoal generates after making charcoal heats with the device 2 of making charcoal through tubular type downwards by high temperature coal ash transfer lime 3 and high temperature coal ash flowrate control valve 4 as thermal barrier is mixed into dry distillation reactor device 8 and provides thermal source for coal dust destructive distillation; Discharge by the flue gas collection chamber 26 of the device 1 of making charcoal the device 1 of making charcoal through II cyclonic separator 25 through the tubular type flue gas 27 generating after device 2 and the device 1 of making charcoal are made charcoal of making charcoal.
The present invention adopts make charcoal device 2 of outer row's semicoke and tubular type to carry out the destructive distillation processing of coal dust raw material with the compound technology of making charcoal of the device 1 of making charcoal.Due to outer row's part semicoke, make make charcoal the device 2 and total load of making charcoal of the device 1 of making charcoal is low, always burn that air quantity declines, the equipment size of device and plant energy consumption reduce of tubular type; Tubular type the make charcoal compound technology of making charcoal of device 1 of device 2-of making charcoal is that do not make charcoal in tubular type is made charcoal device 2 semicoke of regenerating completely enters the device 1 of making charcoal.The Main Function that enters device 1 main air of making charcoal is that appropriate to supplement the main air control of making charcoal device 1 temperature of making charcoal be 650～750 DEG C, and the device 1 air linear speed of making charcoal is 0～1.2m/s, and absolute pressure is 0.10～0.40MPa, and the time of making charcoal is 0～5min.The method can make not overtemperature damage of equipment, reach the object that long period is produced.Adopt the tubular type device 2 of making charcoal to improve the ability of making charcoal of device and the efficiency of making charcoal, reduced the high temperature coal ash reserve of the device 1 of making charcoal, the size of having dwindled device 1 equipment of making charcoal, declines appliance arrangement investment; Adopt the coal dust raw material 14 of particle diameter≤3mm, can ensure raw material and coal ash normal fluidisation and destructive distillation in device; Adopt the resinous shale fine powder raw material of particle diameter≤3mm can obtain higher coal tar yield (coal tar yield account for oily coal dust raw material oleaginousness 85～105%).
Described semicoke heat collector 18 semicoke is cooled to≤80 DEG C of dischargers.
The described interior high temperature coal ash of device 1 temperature of making charcoal is 650～750 DEG C, and the device absolute pressure of making charcoal is that 0.1～0.40MPa, linear speed are that 0～1.2m/s, the time of making charcoal are 0～5min.The main air 23 of device 1 of making charcoal is pressurized air, and the Main Function of this main air 23 is the appropriate main airs of making charcoal that supplement, and reaches the high temperature coal ash dense bed temperature of controlling the device 1 of making charcoal the object of 650～750 DEG C.The air quantity of main air 23 is determined by heat calculation according to the high temperature coal ash reserve of the device 1 of making charcoal and device 1 control target temperature of making charcoal.
Described coal dust feed-pipe 10 entrances are arranged on tubular type device 2 bottoms of making charcoal, charging promotes gas 15 and adopts dry gas or water vapor, gas-operated linear speed in coal dust feed-pipe 10 is 1.0～15.0m/s, the coal dust residence time 1.0～5.0min in feed-pipe 10, and it is between 450～560 DEG C that coal dust charging 14 enters the front temperature control of high temperature coal ash transfer lime 3.
The operational condition of described dry distillation reactor device 8 is: temperature of reaction is 460～560 DEG C, preferably 480～540 DEG C, is preferably 500～520 DEG C; The destructive distillation time is 2～10min, and preferably 3.0～6.0min, is preferably 3.5～4.5min.Coal dust raw material 14 heats by the tubular type device 2 of making charcoal, then contacts mixing with high temperature coal ash, and high temperature coal ash is 0.01～1.5 with coal dust raw material mixed weight ratio, and mixing temperature is 460～560 DEG C.High temperature coal ash and coal dust raw material weight are more definite than the heat calculation when mixing; It is 0.10～0.40MPa that dry distillation reactor device 8 reacts absolute pressure.
The stripping condition of the stripping stage 21 of described dry distillation reactor device 8 is conventional, and stripping medium is hyperthermia and superheating water vapor, and stripping temperature is 480～520 DEG C.
Described semicoke contacts and makes charcoal along tubular type that device 2 is up makes charcoal at the make charcoal wind of making charcoal that device 2 bottoms make charcoal in wind distribution rings 13 with II of tubular type.The adjusting air quantity device 2 charcoal temperature controls of tubular type can being made charcoal of making charcoal are 650～750 DEG C, and the make charcoal air linear speed of device 2 of tubular type is that 1.0～20m/s, the time of making charcoal are 3～40s.The wind of making charcoal can be pressurized air, and when its flow can burn according to semicoke carbon content, required air quantity calculates and determines.
Described coal dust raw material 14 particle diameters≤3mm, oleaginousness (aluminium Zhen method) 5～35%, water content≤15%.In coal chemical technology, be ripe by coal raw material crushing technically to particle diameter≤3mm at present.
Operation and the control process of the technician of coal chemical technology to the dry distillation of coal is clearly, can select aforesaid operations condition according to concrete operations situation.
Comparative example and embodiment
Comparative example
Coal dust feedstock property is in table 1, and the operational condition of destructive distillation device, product distribute in table 2.
Embodiment 1
Embodiment coal dust feedstock property used is in table 3.
Coal dust destructive distillation is carried out on the fluidizer of laboratory, and semicoke adopts tubular type to enter in the device of making charcoal after making charcoal and makes charcoal, and regeneration semicoke enters the device by the main air amount control actuator temperature of making charcoal of making charcoal again.The stripping medium of dry distillation reactor device stripping stage is water vapor, and stripping temperature is 500 DEG C.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device 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, coal dust material feeding tube linear gas velocity, the coal dust material feeding tube residence time, the tubular type of actuator temperature, 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 of making charcoal burns time, the tubular type device linear speed of making charcoal.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device 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, coal dust material feeding tube linear gas velocity, the coal dust material feeding tube residence time, the tubular type of actuator temperature, 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 of making charcoal burns time, the tubular type device linear speed of making charcoal.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device 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, coal dust material feeding tube linear gas velocity, the coal dust material feeding tube residence time, the tubular type of actuator temperature, 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 of making charcoal burns time, the tubular type device linear speed of making charcoal.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device are in table 7.
Embodiment 5
Press embodiment 1, difference is that weight ratio, dry distillation reactor device pyrolysis temperature, dry distillation reactor device destructive distillation time, coal dust material feeding tube linear gas velocity, the coal dust material feeding tube residence time, the tubular type of actuator temperature, 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 of making charcoal burns time, the tubular type device linear speed of making charcoal.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device are in table 8.
Embodiment 6
Press embodiment 1, difference is that weight ratio, dry distillation reactor device pyrolysis temperature, dry distillation reactor device destructive distillation time, coal dust material feeding tube linear gas velocity, the coal dust material feeding tube residence time, the tubular type of actuator temperature, 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 of making charcoal burns time, the tubular type device linear speed of making charcoal.Operational condition, product distribution and the portioned product character of the present embodiment coal dust destructive distillation device are in table 9.
Table 1 coal dust feedstock property (comparative example)
| Title | Numerical value |
| Specific heat, cal/kg. DEG C | 0.264 |
| Oleaginousness, % (aluminium Zhen method) | 14.50 |
| Water content, % | 6.50 |
| Coal ash content, % | 11.40 |
| Size distribution % | |
| ≤0.5mm | 2.0 |
| 0.5-5mm | 11.0 |
| 5-10mm | 16.5 |
| 10-20mm | 26.3 |
| 20-30mm | 44.2 |
Operational condition, the product of table 2 fixed bed coal dried bean noodles distillation unit distribute and portioned product character (comparative example)
Table 3 coal dust feedstock property (embodiment)
| Title | Numerical value |
| Heap ratio, g/ml | 1.06 |
| Specific heat, cal/kg. DEG C | 0.264 |
| Oleaginousness, % (aluminium Zhen method) | 14.50 |
| Water content, % | 6.50 |
| Coal ash content, % | 11.40 |
| Size distribution % | |
| 0-20μm | 6.5 |
| 20-40μm | 5.5 |
| 40-80μm | 6.6 |
| 80-110μm | 8.2 |
| 110-149μm | 10.3 |
| 149-500μm | 19.1 |
| 500-1000μm | 17.0 |
| 1000-1500μm | 15.3 |
| 1500-3000μm | 11.5 |
Operational condition, the product of table 4 coal dust destructive distillation device distribute and portioned product character
Operational condition, the product of table 5 coal dust destructive distillation device distribute and portioned product character
Operational condition, the product of table 6 coal dust destructive distillation device distribute and portioned product character
Operational condition, the product of table 7 coal dust destructive distillation device distribute and portioned product character
Operational condition, the product of table 8 coal dust destructive distillation device distribute and portioned product character
Operational condition, the product of table 9 coal dust destructive distillation device distribute and portioned product character
Claims (28)
1. a coal carbonization method, is characterized in that comprising the steps:
I) the coal dust raw material (14) of particle diameter≤3mm enters and is arranged on after the feed-pipe (10) that tubular type makes charcoal in device (2) under the effect that promotes gas (15), with be mixed into dry distillation reactor device (8) from the high temperature coal ash of the device of making charcoal (1) and carry out destructive distillation, reaction generates the I cyclonic separator (6) of oil gas (22) in dry distillation reactor device (8) and separates, isolated reaction generation oil gas (22) enters fractionating system and carries out fractionation, and isolated semicoke enters Step II);
II) from step I) semicoke the semicoke dense bed (9) and the stripping stage (21) that enter in dry distillation reactor device (8) carry out stripping, after stripping, part semicoke is discharger after heat-obtaining cooling, another part semicoke enters that tubular type makes charcoal that device (2) bottom contacts with the wind of making charcoal and along tubular type up the making charcoal of device (2) of making charcoal, the separating of regenerate afterwards semicoke and flue gas;
III) the regeneration semicoke after separation enters in the high temperature coal ash dense bed of the device of making charcoal (1), charcoal on burning-off regeneration semicoke, the high temperature coal ash that the device (1) of making charcoal generates after making charcoal is mixed into dry distillation reactor device (8) as thermal barrier by high temperature coal ash transfer lime (3) and the coal dust raw material (14) of making charcoal after device (2) heating through tubular type, tubular type make charcoal device (2) and the device of making charcoal (1) make charcoal after flue gas (27) discharger of generation.
2. coal carbonization method according to claim 1, is characterized in that: described a part of semicoke after stripping through heat-obtaining be cooled to≤80 DEG C after discharger.
3. coal carbonization method according to claim 1 and 2, is characterized in that: described a part of semicoke after stripping through heat collector (18) heat-obtaining be cooled to≤80 DEG C enter semicoke blow-down drum (17) discharger.
4. coal carbonization method according to claim 1, is characterized in that: described another part semicoke after stripping enters tubular type device (2) bottom of making charcoal by I semicoke inclined tube (11) and I semicoke flowrate control valve (12).
5. coal carbonization method according to claim 1, it is characterized in that: in described dry distillation reactor device (8), the coal dust raw material dry distillation reactor time is 2～10min, dry distillation reactor temperature is 460～560 DEG C, and dry distillation reactor absolute pressure is 0.10～0.40MPa.
6. coal carbonization method according to claim 1, is characterized in that: water-content≤15 % by weight in described coal dust raw material (14).
7. coal carbonization method according to claim 1, it is characterized in that: coal dust raw material (14) carried out with mixing in high temperature coal ash transfer lime (3) of high temperature coal ash, high temperature coal ash is 0.01～1.5 with coal dust raw material weight ratio, and mixing temperature is 460～560 DEG C.
8. coal carbonization method according to claim 1, is characterized in that: described lifting gas (15) adopts dry gas or water vapor.
9. according to the coal carbonization method described in claim 1 or 8, it is characterized in that: the linear gas velocity of the lifting gas in feed-pipe (10) is 1.0～15.0m/s, coal dust raw material (14) is the residence time 1.0～5.0min in feed-pipe (10), and it is between 450～560 DEG C that coal dust raw material (14) enters the front temperature control of high temperature coal ash transfer lime (3).
10. according to the coal carbonization method described in claim 1 or 4, it is characterized in that: described another part semicoke after stripping enters tubular type and makes charcoal and contact with the wind of making charcoal behind device (2) bottom and along tubular type up the making charcoal of device (2) of making charcoal, supplement the wind of making charcoal and enter in tubular type device (2) middle and upper part of making charcoal.
11. coal carbonization methods according to claim 1, it is characterized in that: tubular type is made charcoal the interior temperature of device (2) between 650～750 DEG C, the linear speed that the wind of making charcoal is made charcoal in device (2) in tubular type is 1.0～20.0m/s, and the time of making charcoal is 3～40s.
12. according to the coal carbonization method described in claim 1 or 10, it is characterized in that: described in the wind of making charcoal be pressurized air.
13. coal carbonization methods according to claim 1, it is characterized in that: the high temperature coal ash dense bed temperature in the device of making charcoal (1) is at 650～750 DEG C, the time of making charcoal in device (1) of making charcoal is 0.1～5min, and absolute pressure is 0.1～0.40MPa.
14. coal carbonization methods according to claim 1, it is characterized in that: the regeneration semicoke after described separation enters in the high temperature coal ash dense bed of the device of making charcoal (1), with the charcoal on main air (23) burning-off regeneration semicoke, main air (23) is pressurized air.
15. 1 kinds for realizing the destructive distillation device of dry distillation of coal method described in claim 1, it is characterized in that: this device comprises the device of making charcoal (1), the tubular type device (2) of making charcoal, feed-pipe (10) and dry distillation reactor device (8), dry distillation reactor device (8) comprises I cyclonic separator (6) and stripping stage (21), the device (1) of making charcoal is connected with dry distillation reactor device (8) by high temperature coal ash transfer lime (3), it is inner and coaxially arrange with it that feed-pipe (10) is positioned at the tubular type device (2) of making charcoal, feed-pipe (10) outlet is connected with high temperature coal ash transfer lime (3), feed-pipe (10) import is arranged on make charcoal device (2) bottom of tubular type, tubular type device (2) top of making charcoal is connected with the device of making charcoal (1), bottom is connected with the stripping stage (21) of dry distillation reactor device (8) bottom by I semicoke inclined tube (11).
16. devices according to claim 15, it is characterized in that: described coal carbonization device also comprises heat collector (18), be arranged at dry distillation reactor device (8) outside, be connected with the stripping stage (21) of dry distillation reactor device (8) bottom by II semicoke inclined tube (20) and setting II semicoke flowrate control valve (19) thereon.
17. devices according to claim 15, is characterized in that: described in make charcoal device (1) by high temperature coal ash transfer lime (3) and high temperature coal ash flowrate control valve (4) be thereon set and be connected with dry distillation reactor device (8).
18. device according to claim 15, is characterized in that: make charcoal device (2) bottom of described tubular type is connected with the stripping stage (21) of dry distillation reactor device (8) bottom by I semicoke inclined tube (11) and setting I semicoke flowrate control valve (12) thereon.
19. devices according to claim 15, is characterized in that: the described tubular type device (2) of making charcoal is provided with two wind distribution rings of making charcoal, and one is arranged at bottom, and in I semicoke inclined tube (11) entrance below; Another is arranged at middle and upper part, and in feed-pipe (10) outlet top.
20. devices according to claim 16, is characterized in that: described heat collector (18) is connected with semicoke blow-down drum (17).
21. devices according to claim 15, is characterized in that: described in the device (1) of making charcoal be arranged on dry distillation reactor device (8) top.
22. according to the device described in claim 15 or 21, it is characterized in that: described in the make charcoal metal shell liner insulating and wearing-resistant lining of device (1).
23. devices according to claim 15, it is characterized in that: it is circular metal tube that described high temperature coal ash transfer lime (3) adopts cross section, diameter of phi 200～3000mm, entrance is arranged on the top of the device of making charcoal (1) high temperature coal ash dense bed, and outlet position is located at the top at semicoke dense bed (9) interface in dry distillation reactor device (8).
24. devices according to claim 15, is characterized in that: described dry distillation reactor device (8) is metal shell liner insulating and wearing-resistant lining.
25. devices according to claim 15, is characterized in that: it is circular metal tube that described feed-pipe (10) adopts cross section, diameter of phi 200～3000mm, and pipeline wall thickness 3～10cm, length is 8～35m.
26. devices according to claim 15, described feed-pipe (10) is arbitrarily angled connection with high temperature coal ash transfer lime (3).
27. devices according to claim 15, is characterized in that: tubular type make charcoal device (2) adopt cross section be circular metal tube, liner insulating and wearing-resistant lining, length is 10～40m, diameter of phi 400～5000mm.
28. devices according to claim 15, is characterized in that: it is characterized in that: the make charcoal diameter ratio of device (2) and feed-pipe (10) of tubular type is 2.5～20.0.
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| CN104099114A (en) * | 2013-04-15 | 2014-10-15 | 中石化洛阳工程有限公司 | Carbonization method for coal |
| CN104178228B (en) * | 2013-05-23 | 2016-08-17 | 中石化洛阳工程有限公司 | A kind of fluidized bed dry distillation method and apparatus of coal dust |
| CN104178184B (en) * | 2013-05-23 | 2016-09-14 | 中石化洛阳工程有限公司 | The fluidized bed dry distillation method and apparatus of coal dust |
| CN104178227B (en) * | 2013-05-23 | 2016-09-14 | 中石化洛阳工程有限公司 | A kind of fluidized bed dry distillation method and device of coal dust |
| CN104862027B (en) * | 2015-04-28 | 2017-03-08 | 袁继海 | A kind of lump coal and fine coal combination drying method for destructive distillation and device |
| CN104962306B (en) * | 2015-06-15 | 2017-03-15 | 天津天绿健科技有限公司 | A kind of method that Coal dressing prepares hydrocarbon oil feedstock |
| CN105938378A (en) * | 2016-05-20 | 2016-09-14 | 江苏盈丰智能工程科技有限公司 | Control device used for coal dry distillation process and control method thereof |
| CN107652997B (en) * | 2017-10-30 | 2023-08-29 | 山东大学 | Powdery semi-coke preparation device and process |
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| CN102031154A (en) * | 2009-09-29 | 2011-04-27 | 惠生工程（中国）有限公司 | Method for comprehensively utilizing lignite |
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