CN103160299A - 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 the 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 resource structures characteristics of the few oil of the rich coal of China have determined the dominant position of coal in energy expenditure, realize that the efficient clean utilization of coal is to solving China's coal burning pollution, oil shortage and realizing that resource, the energy, environment global optimization and Sustainable development are significant.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 the low-temperature pyrolysis process, low-molecular-weight hydrocarbon compound can discharge from coal, can obtain high-quality liquid fuel after hydrotreatment.Produce the process of liquid fuel with coal direct liquefaction or indirect liquefaction and compare, 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.The external-heat Technology is ripe, but thermo-efficiency is low, heat inhomogeneously, and the secondary of volatility product decomposes seriously; Internal heat type technique has overcome the shortcoming of external-heat, by thermal barrier, heat is directly passed to coal, the coal rear generation pyrolytic reaction of being heated.Be divided into again solid heat carrier pyrolysis technique and gaseous heat-carrier pyrolytic process according to the heating medium difference.Solid heat carrier pyrolysis technology utilization high temperature semicoke or other high-temp solid material mix in the pyrolysis chamber with coal, utilize the sensible heat of thermal barrier with pyrolysis of coal, comprise the techniques such as Garrett, Toscoal, LR, DG and ETCH-175.The gaseous heat-carrier pyrolytic process is normally introduced the pyrolysis chamber with the flue gas of fuel combustion, two boiling bed process of representational COED technique, ENCOAL technique and Poland that the strange three sections stoves in Shandong, Fushun stove, the U.S. arranged etc.Patent 200810012528.5 discloses a kind of fluidized bed low temperature dry distillation technological process based on petroleum catalytic cracking technique, and the dry distillation reactor device has adopted the petroleum catalytic cracking reactor, collects fine powder by internal cyclone, and device structure is more complicated.Patent 200810028510.4 discloses a kind of low-temperature pyrolysis technique based on the bubbling bed fluidized-bed reactor, and the volume utilization of bubbling bed reactor is low, and the bottom is without ash releasing tube, and the 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 the 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 of fluidized-bed gasification furnace generation, hydrogen content can reach 30～40%.Therefore, inventor's consideration, the heating gas that produces take vapourizing furnace carries out the low-temperature pyrolysis of coal as thermal barrier, further improve 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 that obtains is good.The technical problem to be solved in the present invention also is 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:
By the top straight length 33 that reducing section 32 is connected with the upper port of described bottom expanding reach 31, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 that is 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;
Be positioned at the middle part of described gas distribution grid 29 and pass the semicoke discharge gate 36 of described cloth air chamber 28 outer walls.
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 the 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, formed by drying and preheating device, low-temperature pyrolysis reactor, vapourizing furnace and carbonization gas after-treatment system, produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, described low-temperature pyrolysis reactor comprises:
By the top straight length 33 that reducing section 32 is connected with the upper port of described bottom expanding reach 31, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 that is 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;
Be positioned at the middle part of described gas distribution grid 29 and pass the semicoke discharge gate 36 of described cloth air chamber 28 outer walls.
Accordingly, the present invention also provides a kind of low-temperature cracking process of low-rank coal, comprising:
Produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, generate with carry out dry distillation reactor after the low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device the carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to enter 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 as gasified raw material and obtains heating gas in fluidized-bed gasification furnace, and controlling gasification temperature is 900～1100 ℃;
Described heating gas and circulation cooled coal gas are mixed to get mixed gas, and controlling temperature is 700～900 ℃.
Preferably, described the 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 carried out drying and preheating, controlling gas speed is 0.2～1m/s, controlling temperature is 150～250 ℃.
Preferably, described low-temperature pyrolysis reactor comprises:
By the top straight length 33 that reducing section 32 is connected with the upper port of described bottom expanding reach 31, straight length 33 tops, described top are provided with carbonizing gas outlet 34;
The cloth air chamber 28 that is 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;
Be positioned at the middle part of described gas distribution grid 29 and pass the semicoke discharge gate 36 of described cloth air chamber 28 outer walls.
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 produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, generates with carry out dry distillation reactor after the low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device 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 produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, can play the effect of partial hydrogenation due to the hydrogen atmosphere of coal gas, 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 macrobead residence time of solid in reactor, improves the 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, and 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 that is 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 the destructive distillation effect; Secondly, this two-section low-temperature dry distillation reactor device is conducive to the solid content that keeps higher 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, and is short in the high temperature section residence time, prevents the secondary polycondensation of tar, and tar yield is high.
Description of drawings
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
The below is clearly and completely described the technical scheme in the embodiment of the present invention, and obviously, described embodiment is only the present invention's part embodiment, rather than whole embodiment.Based on the embodiment in the present invention, those of ordinary skills belong to the scope of protection of the invention not making the every other embodiment that obtains under the creative work prerequisite.
As Fig. 1, Fig. 2 and shown in Figure 3, the invention discloses a kind of fluidized bed low temperature dry distillation system, formed by drying and preheating device 4, low-temperature pyrolysis reactor 8, vapourizing furnace 21 and carbonization gas after-treatment system, produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, Fig. 2 is the structural representation of low-temperature pyrolysis reactor 8, comprising:
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 the 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, the hot flue gas of drying; 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, the 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, the destructive distillation heating gas; The 21st, vapourizing furnace; The 22nd, the gasification cyclonic separator; The 23rd, vaporized chemical; The 24th, the gasification deslagging; The 25th, heating gas; The 26th, the circulation cooled coal gas; The 27th, the import of destructive distillation heating gas; The 28th, the 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, the carbonizing gas outlet; The 35th, solid particulate returning charge mouth; The 36th, the 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; the carbonization gas after-treatment system preferably is 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 the strength flow valve to control the feed back amount and can increase the solid macrobead residence time, improve the tar yield, realize simultaneously the fast pyrogenation of tar, 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 the 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, keep gas uniform to distribute through gas distribution grid 29.Low-rank coal (the granularity＜6mm) add low-temperature pyrolysis reactor 8 by coal inlet 30 of the high-volatile of drying, fragmentation; The macrobead coal dust is protected 31 at the bottom of low-temperature pyrolysis reactor 8 expanding reach and is kept the turbulence fluidized state, less pulverized coal particle is entrained to top straight length 33 by hot gas, fine powder and carbonization gas are discharged from the carbonizing gas outlet 34 of dry distillation reactor device top setting, 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 separates fine powder and carbonizing gas, and the fine powder semicoke is discharged from cyclonic separator, and carbonizing gas send rear system recoveries tar and coal gas; Semicoke in low-temperature pyrolysis reactor 8 is discharged from discharge gate 36.
Can find out from technique scheme, the low-temperature pyrolysis reactor that the present invention adopts adopts fluidization technology take heating gas or flue gas as thermal source, and solids mixing is effective, and heat and mass efficient is high, applicable to the cohesiveness coal.The method produces the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, can play the effect of partial hydrogenation due to the hydrogen atmosphere of coal gas, 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 macrobead residence time of solid in reactor, improves the 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, and solid particulate easily reclaims, and has higher system thermal efficiency; Coordinate with coal gasification, combustion processes, can realize that coal grading transforms, and improves resource utilization.
Accordingly, the present invention also provides a kind of low-temperature cracking process of low-rank coal, comprising:
Produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, generate with carry out dry distillation reactor after the low-rank coal drying and preheating in the low-temperature pyrolysis reactor carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to enter successively primary cyclone behind low-temperature pyrolysis reactor top and secondary cyclone carries out dedusting.
Described the 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 carried out drying 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: through broken, screening, particle diameter is sent into drying and preheating device 4 through coal bunker 1 through feeder 2 less than the fine coal of 8mm with coal, and controlling gas speed is 0.2～1m/s, temperature is 150～250 ℃ coal carried out drying 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 the tar oxygen level, improves the tar calorific value.
Low-rank coal after described drying and preheating is carried out dry distillation reactor and is specially in the 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, enter from dry distillation reactor device 8 bottom cloth air chambers 28, 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 was completed, carbonization gas carried 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 separates the destructive distillation product through gas-liquid separator 15, obtains semi coking tar and high heating value gas; The semicoke 19 that dry distillation reactor generates enters in fluidized-bed gasification furnace 21 as gasified raw material and obtains heating gas, and controlling gasification temperature is 900～1100 ℃; Described heating gas and circulation cooled coal gas are mixed to get 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 the destructive distillation effect; Secondly, this two-section low-temperature dry distillation reactor device is conducive to the solid content that keeps higher 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, and is 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 describe just as further illustrating the features and advantages of the present invention, rather than limiting to the claimed invention.
Adopt the present invention 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 the coal analysis data are as shown in table 1.
At first, raw coal is through broken, screening, and particle diameter is sent into drying and preheating device 4 through coal bunker 1 through feeder 2 less than the fine coal of 8mm, controls 180～210 ℃ of temperature, carries out drying and preheating;
The coal dust of preheating is entered 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, enter from dry distillation reactor device 8 bottom cloth air chambers 28, 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 separates the destructive distillation product through gas-liquid separator 15, 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 after tornado dust collector 22 are removed dust, and part heating gas 20 is as the 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/％) |
Fluidized bed low temperature dry distillation device and operation steps are identical with embodiment 1.Feed coal is 6 grades of Yilans coal, and the coal analysis data are as shown in table 3.Control the raw coal particle diameter 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.The 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 is 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
Fluidized bed low temperature dry distillation device and operation steps are identical with embodiment 1.Feed coal is 32 grades of Yilans coal, and the coal analysis data are as shown in table 5.Control the raw coal particle diameter 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.The 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 the coal analysis data are as shown in table 7.Control the raw coal particle diameter 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.The 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
To the above-mentioned explanation of the disclosed embodiments, make this area professional and technical personnel can realize or use the present invention.Multiple modification to these embodiment will be apparent concerning those skilled in the art, and General Principle as defined herein can be in the situation that do not break away from the spirit or scope of the present invention, realization 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 (10)
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;
By the top straight length (33) that reducing section (32) is connected with the upper port of described bottom expanding reach (31), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) that is 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;
Be positioned at the middle part of described gas distribution grid (29) and pass the semicoke discharge gate (36) of described cloth air chamber (28) outer wall.
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, and described bottom expanding reach (31) is 1 with the Length Ratio of described top straight length (33): (5～20).
3. low-temperature pyrolysis reactor according to claim 1, is characterized in that, 45～75 ° of the angles 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 the aperture is 2～10mm, and percentage of open area is 1～5%.
5. fluidized bed low temperature dry distillation system, it is characterized in that, formed by drying and preheating device, low-temperature pyrolysis reactor, vapourizing furnace and carbonization gas after-treatment system, produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, 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;
By the top straight length (33) that reducing section (32) is connected with the upper port of described bottom expanding reach (31), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) that is 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;
Be positioned at the middle part of described gas distribution grid (29) and pass the semicoke discharge gate (36) of described cloth air chamber (28) outer wall.
6. the low-temperature cracking process of a low-rank coal, is characterized in that, comprising:
Produce the mixed gas of heating gas and circulation cooled coal gas as thermal barrier and the fluidizing agent of dry distillation reactor with vapourizing furnace, generate with carry out dry distillation reactor after the low-rank coal drying and preheating in two-section low-temperature dry distillation reactor device the carbonization gas of carrying coal dust secretly;
The described carbonization gas of carrying coal dust secretly is risen to enter successively primary cyclone behind low-temperature pyrolysis reactor top and secondary cyclone carries out dedusting.
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 as gasified raw material and obtains heating gas in fluidized-bed gasification furnace, and controlling gasification temperature is 900～1100 ℃;
Described heating gas and circulation cooled coal gas are mixed to get mixed gas, and controlling temperature is 700～900 ℃.
9. low-temperature cracking process according to claim 6, is characterized in that, described the 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 carried out drying and preheating, controlling gas speed is 0.2～1m/s, controlling temperature is 150～250 ℃.
10. low-temperature cracking process according to claim 6, is characterized in that, 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;
By the top straight length (33) that reducing section (32) is connected with the upper port of described bottom expanding reach (31), described top straight length (33) top is provided with carbonizing gas outlet (34);
The cloth air chamber (28) that is 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;
Be positioned at the middle part of described gas distribution grid (29) and pass the semicoke discharge gate (36) of described cloth air chamber (28) outer wall.
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| CN110003929A (en) * | 2019-02-01 | 2019-07-12 | 浙江天禄环境科技有限公司 | A kind of method of coal gasification reduction and upgraded coal separation and recovery |
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