CN103160299B - Fluidized bed low-temperature destructive distillation system and low-temperature destructive distillation method of low-rank coal - Google Patents
Fluidized bed low-temperature destructive distillation system and low-temperature destructive distillation method of low-rank coal Download PDFInfo
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Abstract
The invention provides a fluidized bed low-temperature destructive distillation system and a low-temperature destructive distillation method of low-rank coal. According to the method, a mixed gas of hot coal gas produced by a gasification furnace and circulation cold coal gas is adopted as a hot carrier and a fluidizing gas of a destructive distillation reaction. A hydrogen atmosphere of coal gas can provide a partial hydrogenation effect, such that obtained tar has the advantages of high light component content, good quality, high thermal efficiency, and high yield. Also, with the method, a two-stage low-temperature destructive distillation reactor is adopted, such that the retention time of solid particles in the reactor is increased, destructive distillation effect is improved, high solid content in the bed can be maintained, and operation stability can be maintained. The invention also provides a low-temperature destructive distillation reactor. The low-temperature destructive distillation reactor is the two-stage low-temperature destructive distillation reactor, such that the retention time of solid particles in the reactor is increased, and destructive distillation effect is improved. With the two-stage low-temperature destructive distillation reactor, high solid content in the bed can be maintained, and operation stability can be maintained.
Description
Technical field
The present invention relates to derived energy chemical technical field, more particularly, relate to the low-temperature cracking process of a kind of fluidized bed low temperature dry distillation system and low-rank coal.
Background technology
The few oily resource structures feature of the rich coal of China has determined the dominant position of coal in energy expenditure, and the efficient clean utilization that realizes coal is significant to solving China's coal burning pollution, oil shortage and realizing resource, the energy, environment global optimization and Sustainable development.The complex material that coal is comprised of multiple elements such as C, H, O, its agent structure is the macromole aromatic nucleus of polymerization, a certain amount of small molecule hydrocarbon compounds and heterogeneous ring compound are scattered here and there in agent structure.In low-temperature pyrolysis process, low-molecular-weight hydrocarbon compound can discharge from coal, after hydrotreatment, can obtain high-quality liquid fuel.Compare with the process that direct liquefaction or the indirect liquefaction of coal are produced liquid fuel, the low-temperature cracking process production technique of coal is simple, and equipment requirements is low, good economy performance.
Coal low-temperature pyrolysis technique can be divided into external-heat and internal heat type two classes by type of heating.External-heat Technology is ripe, but thermo-efficiency is low, heats inhomogeneously, and the secondary of volatility product decomposes serious; Internal heat type technique has overcome the shortcoming of external-heat, by thermal barrier, heat is directly passed to coal, after coal is heated, pyrolytic reaction occurs.According to heating medium difference, be divided into again solid heat carrier pyrolysis technique and gaseous heat-carrier pyrolytic process.In solid heat carrier pyrolysis technology utilization high temperature semicoke or other high-temp solid material Yu Mei pyrolysis chamber, mix, utilize the sensible heat of thermal barrier by pyrolysis of coal, comprise the techniques such as Garrett, Toscoal, LR, DG and ETCH-175.Gaseous heat-carrier pyrolytic process is normally introduced pyrolysis chamber by the flue gas of fuel combustion, two boiling bed process of representational COED technique, ENCOAL technique and Poland that has the strange three sections of stoves in Shandong, Fushun stove, the U.S. etc.Patent 200810012528.5 discloses a kind of fluidized bed low temperature dry distillation technological process based on petroleum catalytic cracking technique, and dry distillation reactor device has adopted petroleum catalytic cracking reactor, by internal cyclone, collects fine powder, and device structure is more complicated.Patent 200810028510.4 discloses a kind of low-temperature pyrolysis technique based on bubbling bed fluidized-bed reactor, and the volume utilization of bubbling bed reactor is low, and bottom is without ash releasing tube, and macrobead ash discharge is difficult.
The low-temperature pyrolysis of coal under hydrogen atmosphere, can realize the partial hydrogenation of dry-run tar, prevents that free radical polycondensation from generating heavy tar, has advantages of that tar yield is high, light constituent content is high.In addition, in the heating gas that fluidized-bed gasification furnace produces, hydrogen content can reach 30～40%.Therefore, inventor's consideration, the heating gas that the vapourizing furnace of take produces, as thermal barrier carries out the low-temperature pyrolysis of coal, further improves thermo-efficiency and tar yield, improves the economic worth of coal.
Summary of the invention
In view of this, the technical problem to be solved in the present invention is to provide the low-temperature cracking process of a kind of fluidized bed low temperature dry distillation system and low-rank coal, and the method thermo-efficiency is high, tar yield is high, and the quality of coke tar obtaining is good.The technical problem to be solved in the present invention is also to provide a kind of low-temperature pyrolysis reactor, and thermo-efficiency is high, tar yield is high.
In order to solve above technical problem, the invention provides a kind of low-temperature pyrolysis reactor, comprising:
Bottom expanding reach 31; Lay respectively at coal inlet 30 and the solid particulate returning charge mouth 35 of expanding reach 31 upper and lowers, described bottom;
The top straight length 33 being connected with the upper port of described bottom expanding reach 31 by reducing section 32, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 being connected with the lower port of described bottom expanding reach 31 by gas distribution grid 29;
Be arranged at the hot gas import 27 of described cloth air chamber 28 sides;
The semicoke discharge gate 36 of described cloth air chamber 28 outer walls is also passed at the middle part that is positioned at described gas distribution grid 29.
Preferably, described bottom expanding reach 31 is (1.2～3) with the caliber ratio of described top straight length 33: 1, and described bottom expanding reach 31 is 1 with the Length Ratio of described top straight length 33: (5～20).
Preferably, 45～75 ° of the angles of described reducing section 32 and horizontal plane.
Preferably, described gas distribution grid 29 is porous plate, and aperture is 2～10mm, and percentage of open area is 1～5%.
Accordingly, the present invention also provides a kind of fluidized bed low temperature dry distillation system, by drying and preheating device, low-temperature pyrolysis reactor, vapourizing furnace and carbonization gas after-treatment system, formed, the vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, and described low-temperature pyrolysis reactor comprises:
Bottom expanding reach 31; Lay respectively at coal inlet 30 and the solid particulate returning charge mouth 35 of expanding reach 31 upper and lowers, described bottom;
The top straight length 33 being connected with the upper port of described bottom expanding reach 31 by reducing section 32, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 being connected with the lower port of described bottom expanding reach 31 by gas distribution grid 29;
Be arranged at the hot gas import 27 of described cloth air chamber 28 sides;
The semicoke discharge gate 36 of described cloth air chamber 28 outer walls is also passed at the middle part that is positioned at described gas distribution grid 29.
Accordingly, the present invention also provides a kind of low-temperature cracking process of low-rank coal, comprising:
The vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, by carry out dry distillation reactor after low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device, generates the carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to and enters successively primary cyclone behind low-temperature pyrolysis reactor top and secondary cyclone carries out dedusting.
Preferably, the temperature of described dry distillation reactor is 450～600 ℃, and the gas speed of described two-section low-temperature dry distillation reactor device is 2～10m/s.
Preferably, also comprise:
The semicoke that dry distillation reactor is generated enters in fluidized-bed gasification furnace and obtains heating gas as gasified raw material, and controlling gasification temperature is 900～1100 ℃;
Described heating gas and circulation cooled coal gas are mixed to get to mixed gas, and controlling temperature is 700～900 ℃.
Preferably, described low-rank coal drying and preheating is specially:
Take hot flue gas as drying medium, low-rank coal is sent in drying and preheating device 4 coal is dried and preheating, controlling gas speed is 0.2～1m/s, and controlling temperature is 150～250 ℃.
Preferably, described low-temperature pyrolysis reactor comprises:
Bottom expanding reach 31; Lay respectively at coal inlet 30 and the solid particulate returning charge mouth 35 of expanding reach 31 upper and lowers, described bottom;
The top straight length 33 being connected with the upper port of described bottom expanding reach 31 by reducing section 32, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 being connected with the lower port of described bottom expanding reach 31 by gas distribution grid 29;
Be arranged at the hot gas import 27 of described cloth air chamber 28 sides;
The semicoke discharge gate 36 of described cloth air chamber 28 outer walls is also passed at the middle part that is positioned at described gas distribution grid 29.
The invention provides the low-temperature cracking process of a kind of fluidized bed low temperature dry distillation system and low-rank coal, the method is usingd vapourizing furnace and is produced the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, by carry out dry distillation reactor after low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device, generates the carbonization gas of carrying coal dust secretly; The described carbonization gas of carrying coal dust secretly is risen to dedusting behind low-temperature pyrolysis reactor top.Compared with prior art, the method is usingd vapourizing furnace and is produced the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, because the hydrogen atmosphere of coal gas can play the effect of partial hydrogenation, thereby gained tar light constituent content is high, quality is good, and thermo-efficiency is high, tar yield is high.In addition, the method adopts two-section low-temperature dry distillation reactor device, increases the residence time of macrobead solid in reactor, improves destructive distillation effect, is conducive to the solid content that keeps higher in bed and the stability that keeps operation.And the method treatment capacity is large, solid particulate easily reclaims, and has higher system thermal efficiency.
In addition, the present invention also provides a kind of low-temperature pyrolysis reactor, comprises bottom expanding reach 31 and top straight length 33 being connected with the upper port of bottom expanding reach 31 by reducing section 32 etc.Compared with prior art, because this low-temperature pyrolysis reactor is two-section low-temperature dry distillation reactor device, increase the residence time of macrobead solid in reactor, improved destructive distillation effect; Secondly, this two-section low-temperature dry distillation reactor device is conducive to keep higher solid content in bed, keeps the stability of operation; Again, this structure is conducive to the fast pyrogenation of tar, and tar is easily taken out of fast by gas, short in the high temperature section residence time, prevents the secondary polycondensation of tar, and tar yield is high.
Accompanying drawing explanation
Fig. 1 is the structural representation of circulating fluidized bed low-temperature pyrolysis reactor of the present invention;
Fig. 2 is the structural representation of low-temperature pyrolysis reactor of the present invention;
Fig. 3 is the structural representation of fluidized bed low temperature dry distillation reactor and after-treatment system.
Embodiment
Below the technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is only the present invention's part embodiment, rather than whole embodiment.Embodiment based in the present invention, those of ordinary skills, not making the every other embodiment obtaining under creative work prerequisite, belong to the scope of protection of the invention.
As shown in Figure 1, Figure 2 and Figure 3, the invention discloses a kind of fluidized bed low temperature dry distillation system, by drying and preheating device 4, low-temperature pyrolysis reactor 8, vapourizing furnace 21 and carbonization gas after-treatment system, formed, the vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, Fig. 2 is the structural representation of low-temperature pyrolysis reactor 8, comprising:
Bottom expanding reach 31; Lay respectively at coal inlet 30 and the solid particulate returning charge mouth 35 of bottom expanding reach 31 upper and lowers; The top straight length 33 being connected with the upper port of bottom expanding reach 31 by reducing section 32, straight length 33 tops in top are provided with carbonizing gas outlet 34; The cloth air chamber 28 being connected with the lower port of bottom expanding reach 31 by gas distribution grid 29; Be arranged at the hot gas import 27 of cloth air chamber 28 sides; Be positioned at gas distribution grid 29 middle parts and also pass the semicoke discharge gate 36 of cloth air chamber 28 outer walls.
The low-temperature pyrolysis reactor 8 that the present invention adopts is two-section low-temperature dry distillation reactor device, and its middle and lower part expanding reach 31 is preferably (1.2～3) with the caliber ratio of top straight length 33: 1, more preferably (1.5～3): 1; Bottom expanding reach 31 is preferably 1 with the length of top straight length 33: (5～20), more preferably 1: (8～15).In addition, reducing section 32 is preferably 45～75 ° with the angle of horizontal plane.Gas distribution grid 29 is porous plate, and aperture is preferably 2～10mm, and percentage of open area is 1～5%.
Fig. 1 is the structural representation of circulating fluidized bed low-temperature pyrolysis reactor of the present invention, wherein, the 1st. coal bunker; The 2nd, feeder; The 3rd, be dried and use hot flue gas; The 4th, the drying and preheating device of coal; The 5th, dry cyclonic separator; The 6th, dry waste gas; The 7th, the dry fine breeze of collecting; The 8th, dry distillation reactor device; The 9th, primary cyclone; The 10th, secondary cyclone; The 11st, finely-ground coke; The 12nd, water wash column; The 13rd, washes; The 14th, washing water; The 15th, gas-liquid separator; The 16th, carbonization gas; The 17th, tar; The 18th, waste water; The 19th, Pyrolysis Char; The 20th, destructive distillation heating gas; The 21st, vapourizing furnace; The 22nd, gasification cyclonic separator; The 23rd, vaporized chemical; The 24th, gasification deslagging; The 25th, heating gas; The 26th, circulation cooled coal gas; The 27th, the import of destructive distillation heating gas; The 28th, cloth air chamber; The 29th, gas distribution grid; The 30th, coal inlet; The 31st, dry distillation reactor device expanding reach; The 32nd, dry distillation reactor device reducing section; The 33rd, dry distillation reactor device straight length; The 34th, carbonizing gas outlet; The 35th, solid particulate returning charge mouth; The 36th, Pyrolysis Char discharge gate.
As shown in Figure 3; structural representation for fluidized bed low temperature dry distillation reactor of the present invention and after-treatment system; carbonization gas after-treatment system is preferably comprised of primary cyclone 9, secondary cyclone 10, standpipe 37 and solid particulate feeding back device 38, and primary cyclone 9 is connected with low-temperature pyrolysis reactor 8 respectively with solid particulate feeding back device 38.Above-mentioned solid particulate feeding back device is non-mechanical strength flow valve, can be loop seal, L valve, J valve.Adopt strength flow valve to control feed back amount and can increase the solid macrobead residence time, improve tar yield, realize the fast pyrogenation of tar simultaneously, and product tar easily taken out of fast by gas, short in the high temperature section residence time, prevent the secondary polycondensation of tar.
In figure 3, material flow A is coal gas of high temperature or flue gas; B is coal dust; C is carbonizing gas; D is semicoke fine powder; E is the fluidizing agent of feeding back device; F is Pyrolysis Char.In low-temperature pyrolysis reactor working process, coal gas of high temperature or flue gas A are entered in cloth air chamber 28 by hot gas import 27, through gas distribution grid 29, keep gas uniform to distribute.The low-rank coal (granularity < 6mm) of the high-volatile of drying, fragmentation adds low-temperature pyrolysis reactor 8 by coal inlet 30; Macrobead coal dust is protected 31 at the bottom of low-temperature pyrolysis reactor 8 expanding reach and is kept turbulence fluidized state, less pulverized coal particle is entrained to top straight length 33 by hot gas, the carbonizing gas outlet 34 that fine powder and carbonization gas arrange from dry distillation reactor device top is discharged, after primary cyclone 9 gas solid separation, particle returns to the further destructive distillation of low-temperature pyrolysis reactor 8 by particles circulating standpipe 37 and solid particulate feeding back device 38 successively; The carbonizing gas of entrained fines enters secondary cyclone 10 again, further separated fine powder and carbonizing gas, and fine powder semicoke is discharged from cyclonic separator, and carbonizing gas send rear system recoveries burnt oil and gas; Semicoke in low-temperature pyrolysis reactor 8 is discharged from discharge gate 36.
From technique scheme, can find out, it is thermal source that the low-temperature pyrolysis reactor that the present invention adopts be take heating gas or flue gas, adopts fluidization technology, and solids mixing is effective, and heat and mass efficiency is high, applicable to cohesiveness coal.The method is usingd vapourizing furnace and is produced the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, because the hydrogen atmosphere of coal gas can play the effect of partial hydrogenation, thereby gained tar light constituent content is high, and quality is good, and thermo-efficiency is high, tar yield is high.In addition, the method adopts two-section low-temperature dry distillation reactor device, increases the residence time of macrobead solid in reactor, improves destructive distillation effect, is conducive to the solid content that keeps higher in bed and the stability that keeps operation.And the method treatment capacity is large, solid particulate easily reclaims, and has higher system thermal efficiency; Coordinate with coal gasification, combustion processes, can realize coal grading and transform, improve resource utilization.
Accordingly, the present invention also provides a kind of low-temperature cracking process of low-rank coal, comprising:
The vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, by carry out dry distillation reactor after low-rank coal drying and preheating in low-temperature pyrolysis reactor, generates the carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to and enters successively primary cyclone behind low-temperature pyrolysis reactor top and secondary cyclone carries out dedusting.
Described low-rank coal drying and preheating is specially: take hot flue gas as drying medium, low-rank coal is sent in drying and preheating device 4 coal is dried and preheating, controlling gas speed is 0.2～1m/s, controlling temperature is 150～250 ℃, said temperature can improve heat transfer rate and drying effect, and reduces the energy consumption of retort process.More specifically, also step comprises: by coal, through broken, screening, particle diameter is less than the fine coal of 8mm and through feeder 2, sends into drying and preheating device 4 through coal bunker 1, and controlling gas speed is 0.2～1m/s, temperature is 150～250 ℃ coal is dried and preheating, and preferably adopting hot flue gas is drying medium.This drying and preheating step reduces destructive distillation institute heat requirement, and the part decarboxylation of part warm can reach the effect that removes oxy radical simultaneously, reduces tar oxygen level, improves tar calorific value.
Low-rank coal after described drying and preheating is carried out dry distillation reactor and is specially in low-temperature pyrolysis reactor: the coal dust of preheating enters dry distillation reactor device 8, heating gas 20 from vapourizing furnace mixes with circulation cooled coal gas 26, regulate 700～900 ℃ of gas temperatures, thermal barrier as dry distillation reactor, from dry distillation reactor device 8 bottom cloth air chambers 28, enter, carry coal dust and move upward, the temperature of described dry distillation reactor is preferably 450～600 ℃, and the gas speed of described low-temperature pyrolysis reactor is preferably 2～10m/s.
After above-mentioned steps completes, carbonization gas carries coke powder and enters primary cyclone 9, and the coke powder circulation of collection enters the further degree of depth destructive distillation of dry distillation reactor device, and carbonization gas enters secondary cyclone 10, removes coal dust; Gas after just dedusting enters water wash column 12, further removes dust, controls 60～80 ℃ of water wash column gas outlet temperatures;
Carbonization gas after washing is through gas-liquid separator 15, and separated destructive distillation product, obtains semi coking tar and high heating value gas; The semicoke 19 that dry distillation reactor generates enters in fluidized-bed gasification furnace 21 and obtains heating gas as gasified raw material, and controlling gasification temperature is 900～1100 ℃; Described heating gas and circulation cooled coal gas are mixed to get to mixed gas, and controlling temperature is 700～900 ℃.Described vapourizing furnace is fluidized-bed gasification furnace, and vaporized chemical is the gas mixture of water vapour and oxygen or air.
The inventive method has advantages of that coal adaptability is strong, thermo-efficiency is high, tar yield is high, quality of coke tar is good, simple in structure, throughput is large.Because this low-temperature pyrolysis reactor is two-section low-temperature dry distillation reactor device, increased the residence time of macrobead solid in reactor, improve destructive distillation effect; Secondly, this two-section low-temperature dry distillation reactor device is conducive to keep higher solid content in bed, keeps the stability of operation; Again, change the fast pyrogenation that structure is conducive to tar, tar is easily taken out of fast by gas, short in the high temperature section residence time, prevents the secondary polycondensation of tar, and tar yield is high.
In order to further illustrate technical scheme of the present invention, below in conjunction with embodiment, the preferred embodiment of the invention is described, but should be appreciated that these are described is for further illustrating the features and advantages of the present invention, rather than limiting to the claimed invention.
Embodiment 1
Adopt the present invention's fluidized bed low temperature dry distillation system as shown in the figure, fluidised bed drying preheater diameter 200mm, high 3000mm; Low-temperature pyrolysis reactor top inside diameter of straight pipe section 50mm, bottom expanding reach internal diameter 80mm, height overall 12000mm; Fluidized-bed gasification furnace diameter 200mm, high 4000mm.Feed coal is six grades of Yilans coal, and coal analysis data are as shown in table 1.
First, raw coal is through broken, screening, and particle diameter is less than the fine coal of 8mm and through feeder 2, sends into drying and preheating device 4 through coal bunker 1, controls 180～210 ℃ of temperature, is dried and preheating;
The coal dust of preheating is entered to dry distillation reactor device 8, heating gas 20 from vapourizing furnace mixes with circulation cooled coal gas 26, regulate 750～800 ℃ of gas temperatures, thermal barrier as dry distillation reactor, from dry distillation reactor device 8 bottom cloth air chambers 28, enter, carry coal dust and move upward, control 470～500 ℃ of pyrolysis temperatures and carry out dry distillation reactor;
Carbonization gas carries coke powder and enters primary cyclone 9, and the coke powder circulation of collection enters the further degree of depth destructive distillation of dry distillation reactor device, and carbonization gas enters secondary cyclone 10, removes coal dust;
Gas after just dedusting enters water wash column 12 and further removes dust, controls 70～80 ℃ of water wash column gas outlet temperatures; Carbonization gas after washing is through gas-liquid separator 15, and separated destructive distillation product, obtains semi coking tar and high heating value gas; Destructive distillation product semicoke 19 enters vapourizing furnace 21, controls 1000～1050 ℃ of gasification temperatures, take air and water vapour as vaporized chemical, heating gas is produced in gasification, heating gas is removed after dust through tornado dust collector 22, and part heating gas 20 is as destructive distillation thermal source, and part heating gas 25 send aftertreatment to utilize system.
Heating gas consists of: H
2content 13～16%, CO content 11～14%, N
2content 45～48%, CH
4content 1～2%, CO
2content 8～12%, H
2o content 12～15%.The productive rate 11.8% of low-temperature pyrolysis tar, char yeild 66.4%, semi coking tar proportion 1.10g/ml.The analysis of distillation process of semicoke character and tar as shown in Table 1 and Table 2.
Work point and first divided data of the six grades of coals in Yilan that table 1 the present embodiment adopts
The analysis of distillation process of table 2 semi coking tar
| Temperature (℃) | ＜100 | 100～170 | 170～230 | 230～300 | Residual | Loss |
| Yield | 12.3 | 21.8 | 8.2 | 28.6 | 20.2 | 8.9 |
| (WT/％) |
Embodiment 2
Fluidized bed low temperature dry distillation device and operation steps are identical with embodiment 1.Feed coal is 6 grades of Yilans coal, and coal analysis data are as shown in table 3.Control raw coal particle diameter and be less than 8mm, 200～230 ℃ of the drying and preheating temperature of coal, 520～550 ℃ of low-temperature pyrolysis temperature, 1000～1050 ℃ of gasification temperatures, other operational condition is identical with embodiment 1.Destructive distillation heating gas consists of: H
2content 13～16%, CO content 11～14%, N
2content 45～48%, CH
4content 1～2%, CO
2content 8～12%, H
2o content 14～16%.The productive rate 12.3% of low-temperature pyrolysis tar, char yeild 66.0%, semi coking tar proportion 1.21g/ml.The analysis of distillation process of semicoke character and tar as shown in Table 3 and Table 4.
Work point and first divided data of the six grades of coals in Yilan that table 3 the present embodiment adopts
The analysis of distillation process of table 4 semi coking tar
Embodiment 3
Fluidized bed low temperature dry distillation device and operation steps are identical with embodiment 1.Feed coal is 32 grades of Yilans coal, and coal analysis data are as shown in table 5.Control raw coal particle diameter and be less than 8mm, 200～230 ℃ of the drying and preheating temperature of coal, 500～520 ℃ of low-temperature pyrolysis temperature, 1000～1050 ℃ of gasification temperatures, other operational condition is identical with embodiment 1.Destructive distillation heating gas consists of: H
2content 10～14%, CO content 10～12%, N
2content 48～50%, CH
4content 0～1%, CO
2content 10～12%, H
2o content 12～15%.The productive rate 7.3% of low-temperature pyrolysis tar, char yeild 67.8%, semi coking tar proportion 1.15g/ml.The analysis of distillation process of semicoke character and tar is as shown in table 5 and table 6.
Work point and first divided data of the six grades of coals in Yilan that table 5 the present embodiment adopts
The analysis of distillation process of table 6 semi coking tar
Embodiment 4
Fluidized bed low temperature dry distillation device and operation steps are identical with embodiment 1.Feed coal is 32 grades of Yilans coal, and coal analysis data are as shown in table 7.Control raw coal particle diameter and be less than 8mm, 200～230 ℃ of the drying and preheating temperature of coal, 550～580 ℃ of low-temperature pyrolysis temperature, 1000～1050 ℃ of gasification temperatures, other operational condition is identical with embodiment 1.Destructive distillation heating gas consists of: H
2content 10～14%, CO content 10～12%, N
2content 48～50%, CH
4content 0～1%, CO
2content 10～12%, H
2o content 12～15%.The productive rate 8.2% of low-temperature pyrolysis tar, char yeild 66.6%, semi coking tar proportion 1.25g/ml.The analysis of distillation process of semicoke character and tar is as shown in table 7 and table 8.
Work point and first divided data of the six grades of coals in Yilan that table 7 the present embodiment adopts
The analysis of distillation process of table 8 semi coking tar
Above-mentioned explanation to the disclosed embodiments, makes professional and technical personnel in the field can realize or use the present invention.To the multiple modification of these embodiment, will be apparent for those skilled in the art, General Principle as defined herein can, in the situation that not departing from the spirit or scope of the present invention, realize in other embodiments.Therefore, the present invention will can not be restricted to these embodiment shown in this article, but will meet the widest scope consistent with principle disclosed herein and features of novelty.
Claims (9)
1. a low-temperature pyrolysis reactor, is characterized in that, comprising:
Bottom expanding reach (31); Lay respectively at coal inlet (30) and the solid particulate returning charge mouth (35) of described bottom expanding reach (31) upper and lower;
The top straight length (33) being connected with the upper port of described bottom expanding reach (31) by reducing section (32), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) being connected with the lower port of described bottom expanding reach (31) by gas distribution grid (29);
Be arranged at the hot gas import (27) of described cloth air chamber (28) side;
The semicoke discharge gate (36) of described cloth air chamber (28) outer wall is also passed at the middle part that is positioned at described gas distribution grid (29).
2. low-temperature pyrolysis reactor according to claim 1, it is characterized in that, described bottom expanding reach (31) is (1.2～3) with the caliber ratio of described top straight length (33): 1, described bottom expanding reach (31) is 1:(5～20 with the Length Ratio of described top straight length (33)).
3. low-temperature pyrolysis reactor according to claim 1, is characterized in that, the angle 45～75o of described reducing section (32) and horizontal plane.
4. low-temperature pyrolysis reactor according to claim 1, is characterized in that, described gas distribution grid (29) is porous plate, and aperture is 2～10mm, and percentage of open area is 1～5%.
5. a fluidized bed low temperature dry distillation system, it is characterized in that, by drying and preheating device, low-temperature pyrolysis reactor, vapourizing furnace and carbonization gas after-treatment system, formed, the vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, and described low-temperature pyrolysis reactor comprises:
Bottom expanding reach (31); Lay respectively at coal inlet (30) and the solid particulate returning charge mouth (35) of described bottom expanding reach (31) upper and lower;
The top straight length (33) being connected with the upper port of described bottom expanding reach (31) by reducing section (32), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) being connected with the lower port of described bottom expanding reach (31) by gas distribution grid (29);
Be arranged at the hot gas import (27) of described cloth air chamber (28) side;
The semicoke discharge gate (36) of described cloth air chamber (28) outer wall is also passed at the middle part that is positioned at described gas distribution grid (29).
6. a low-temperature cracking process for low-rank coal, is characterized in that, comprising:
The vapourizing furnace of usining produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor, by carry out dry distillation reactor after low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device, generates the carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to and enters successively primary cyclone behind low-temperature pyrolysis reactor top and secondary cyclone carries out dedusting;
Described low-temperature pyrolysis reactor comprises:
Bottom expanding reach (31); Lay respectively at coal inlet (30) and the solid particulate returning charge mouth (35) of described bottom expanding reach (31) upper and lower;
The top straight length (33) being connected with the upper port of described bottom expanding reach (31) by reducing section (32), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) being connected with the lower port of described bottom expanding reach (31) by gas distribution grid (29);
Be arranged at the hot gas import (27) of described cloth air chamber (28) side;
The semicoke discharge gate (36) of described cloth air chamber (28) outer wall is also passed at the middle part that is positioned at described gas distribution grid (29).
7. low-temperature cracking process according to claim 6, is characterized in that, the temperature of described dry distillation reactor is 450～600 ℃, and the gas speed of described two-section low-temperature dry distillation reactor device is 2～10m/s.
8. low-temperature cracking process according to claim 6, is characterized in that, also comprises:
The semicoke that dry distillation reactor is generated enters in fluidized-bed gasification furnace and obtains heating gas as gasified raw material, and controlling gasification temperature is 900～1100 ℃;
Described heating gas and circulation cooled coal gas are mixed to get to mixed gas, and controlling temperature is 700～900 ℃.
9. low-temperature cracking process according to claim 6, is characterized in that, described low-rank coal drying and preheating is specially:
Take hot flue gas as drying medium, low-rank coal is sent in drying and preheating device (4) coal is dried and preheating, controlling gas speed is 0.2～1m/s, and controlling temperature is 150～250 ℃.
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