CN103031135A - Fluidized bed hierarchical coal pyrolysis reactor and coal pyrolysis method - Google Patents
Fluidized bed hierarchical coal pyrolysis reactor and coal pyrolysis method Download PDFInfo
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Abstract
The invention discloses a fluidized bed hierarchical coal pyrolysis reactor. The fluidized bed hierarchical coal pyrolysis reactor comprises a pyrolysis chamber, a separating wall, a pyrolytic gas waste heat recovery device, a coal conveying device, a large granule outlet, a mixed material outlet and an ash conveying device, wherein the pyrolysis chamber comprises a low-temperature pyrolysis chamber and a high-temperature pyrolysis chamber. The invention further discloses a method for performing coal pyrolysis by using the device. By the method, the yield of gas is high, the yield of tar is low, high-efficiency and complete pyrolysis of coal is realized, the gas flow is less fluidized, and excellent fluidized heat exchange and conveying of coal, semicoke and circulating ash are realized, so that energy consumption and heat loss caused by fluidized gas are reduced. Low-temperature pyrolytic gas and high-temperature pyrolytic gas are mixed, so secondary pyrolysis of the lightweight tar of the low-temperature pyrolytic gas is realized, the yield of the pyrolytic gas is increased and the amount of the tar is reduced; and the temperature of the medium-temperature gas after mixing is reduced compared with the pyrolysis final temperature of the coal pyrolysis reactor, so the capacity and the flowing resistance of the pyrolytic gas waste heat recovery device can be reduced, the cost of equipment materials is reduced and the reliability of the equipment is improved.
Description
Technical field
The present invention relates to the pyrolysis of coal technical field, be specifically related to a kind of fluidized bed classification pyrolysis of coal reactor and pyrolysis of coal method.
Background technology
Current pyrolysis of coal technology has multiple application purpose, thereby also adopts different pyrolytic processes.The pyrolysis that has is exactly to utilize the heat of coal combustion that the fugitive constituent in the coal is separated out, just to directly obtaining coke or semicoke; Compare coal and coke, the fugitive constituent in the coal has higher utility value mostly.Take coal derived energy chemical as main pyrolytic process, mainly in order to produce tar and Hydrogenation oil fuel, the pyrolysis gas of pyrolysis generation directly burns usually needs for pyrolysis heat, and this technique utilizes the application in field comparatively extensive with inferior coal.Be utilized as main Poly-generation pyrolytic process with combustion power generation, generally produce tar as major product, the byproduct pyrolysis gas directly burns for the producing steam generating; Another pyrolysis of coal is that to improve generating efficiency be purpose, pyrolytic process is to produce pyrolysis gas as main, the semicoke that produces except pyrolysis produces the steam-electric power by burning, and the pyrolysis gas of generation also can improve whole coal power generation efficient by gas combustion-gas vapor combined cycle.
Pyrolysis of coal is the utilization object mainly with the higher low-disintegration coal of fugitive constituent greatly, the low-quality pit ash is large, ash fusion point is low, semicoke calorific value after the pyrolysis is low, if the high temperature semicoke after the pyrolysis is used for the burning of pulverized coal firing boiler, not only need the cooling of high temperature semicoke, increase the pulverized coal preparation system cost, also can bring the serious problems such as stable burning, combustion zone slagging scorification and heating surface wear, simultaneously the capacity of the supporting fly-ash separator of coal-powder boiler, grey transport process system also needs greatly to improve.Thereby for the system of the direct combustion power generation of pyrolysis product semicoke should not will being adopted the special pyrolysis of independent pyrolysis oven, but pyrolysis system and firing system should be combined.
No matter with gas as thermal barrier or the heat of pyrolysis of coal is provided as thermal barrier with solid, all need thermal barrier and coal to carry out efficient heat exchange, the exchange capability of heat of the pyrolysis scheme of employing down-flow fluidized bed using ECT, moving-bed, drum-type and mechanical agitation type hybrid heater is lower, other problem is also more, solves also to be difficult for.Because the mutual heat transfer condition of different media in fluidized-bed layer is splendid, thereby utilizes fluid bed heat analytical system and equipment comparatively simple, better results.
For the system that the pyrolysis product semicoke directly will be burnt, pyrolysis heat can be provided by the high-temp circulating ash that the circular fluid bed temperature reaches more than 800 ℃, high temperature semicoke after the pyrolysis directly enters the fluidized-bed combustion boiler burning with circulating ash, reduce the technique of semicoke high temperature conveying and UTILIZATION OF VESIDUAL HEAT IN, equipment and flow process are comparatively simple.
Tradition fluidized-bed pyrolytic process of coal all is that to produce tar be main purpose, obtains preferably coal utilization comprehensive benefit by producing more high-quality tar.Such processing requirement produces the low temperature tar light oil, thereby pyrolysis temperature can not be too high, usually is controlled at below 600 ℃.If utilize the circulating ash of circular fluid bed as thermal barrier, carry out under suitable low temperature in order to control in the fluidized bed pyrolysis reactor pyrolytic reaction, this pyrolytic process only need to be controlled the part high-temp circulating ash is entered fluidized-bed reactor, and other circulating ash is directly returned fluidized-bed combustion boiler.For most coals, if take full advantage of the fugitive constituent of coal, need under higher temperature, just can finish the abundant pyrolysis of coal, produce simultaneously more a high proportion of pyrolysis gas.But methane content is few in the pyrolysis gas of the direct high temperature pyrolysis of coal, and hydrogen richness is many, and this pyrolysis coal gas is unfavorable for that gas turbine group is in economic and safe operating mode operation.
Summary of the invention
The objective of the invention is to produce the pyrolysis gas than good quality that how suitable gas turbine combustion needs by adopting fluidized-bed to carry out the coal grading pyrolytic process, can ensureing, can realize again the abundant pyrolysis of coal, improve the comprehensive benefit that pyrolysis of coal utilizes.
In order to solve this technical problem, pyrolytic process core of the present invention is the fluidized-bed reactor classification setting that pyrolysis is used, coal is at first in the indoor pyrolysis of carrying out under the low temperature of first step fluidized bed pyrolysis, and then enters that the next stage fluidized bed pyrolysis is indoor carries out pyrolysis under the comparatively high temps.Pyrolysis heat is provided by the circulating ash of circulating fluidized bed boiler separator outlet, and all circulating ash all enters fluidized bed classification pyrolysis of coal reactor and participates in pyrolysis.
Described fluidized-bed reactor comprises pyrolysis chamber, divider wall 5, defeated device for coal 11, the outlet of macrobead material, compound outlet; Described pyrolysis chamber comprises low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4.
Separate by divider wall 5 described low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4, and described low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 are connected in the upper and lower of divider wall 5 respectively.
Optionally, the height of described divider wall 5 is higher than the emulsion zone height of two pyrolysis chambers.
Optionally, the bottom air distribution plate of described low temperature pyrogenation chamber 14 is a little more than the bottom air distribution plate of high temperature pyrolysis chamber 4, can guarantee that semicoke and circulating ash that low temperature pyrogenation chamber 14 is produced are delivered into high temperature pyrolysis chamber 4, thereby reduce energy consumption and thermosteresis that fluidized gas is brought.
The bottom air distribution plate of described low temperature pyrogenation chamber is used for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of described high temperature pyrolysis chamber is used for the air inlet of high temperature pyrolysis chamber fluidized gas.
The main body of low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 all is the up big and down small taper in cross section, can be under less fluidized gas flow, the air-flow velocity that ensures the bottom, pyrolysis chamber is higher, make the coal of greater particle size and semicoke in the abundant fluidisation in bottom, pyrolysis chamber, can ensure simultaneously that the air-flow velocity of separating top, hot cell reduces gradually, strengthen grain fluidized internal recycle amount, increase coal, semicoke and the high temperature circulation ash particle of small particle size in the emulsion zone residence time, be beneficial to abundant heat exchange and pyrolysis; By the discharge time of (the material valve on the discharge nozzle of bottom) control bottom macrobead material 2, can control the pyrolysis time of macrobead material.
Optionally, described defeated device for coal 11 and pyrolysis gas waste-heat recovery device are arranged in the top in the fluidized bed coal pyrolysis reactor pyrolysis chamber, and the separation shutoff by the pyrolyzing coal 10 that transports on it, the top of low temperature pyrogenation chamber 14 and pyrolysis gas waste-heat recovery device 9 are not directly linked.
Optionally, described device also comprises the pyrolysis gas waste-heat recovery device, and it is positioned at the top of high temperature pyrolysis chamber 4, and is connected with 4 tops, high temperature pyrolysis chamber.
The main body of described low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 all is the up big and down small taper in cross section, and low temperature pyrogenation chamber 14 is connected with the ash inlet tube of high-temp circulating ash 12 at bed of material emulsion zone.
Optionally, this ash inlet tube is provided with ash conveying device 13, and this ash conveying device can play the isolating seal effect, avoids the air-flow of low temperature pyrogenation chamber 14 to move back to ash inlet tube.
Described high temperature pyrolysis chamber arranges the compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the less pyrolysis product semicoke of most of high-temp circulating ash and particle diameter, be provided with the compound outlet in bed of material emulsion zone bottom, be used for the discharging of the compound of the larger pyrolysis product semicoke of small part high-temp circulating ash and particle diameter.
The process of utilizing said apparatus to carry out pyrolysis of coal comprises:
Pyrolyzing coal 10 is successively through entering low temperature pyrogenation chamber 14 behind pyrolysis gas waste-heat recovery device 9 and the defeated device for coal 11; High-temp circulating ash 12 from circular fluid bed enters low temperature pyrogenation chamber 14 via ash conveying device 13.
Under the effect of the low temperature pyrogenation chamber fluidized gas 15 that is entered low temperature pyrogenation chamber 14 by bottom, low temperature pyrogenation chamber air distribution plate, pyrolyzing coal 10 carries out the low temperature fluidisation with high-temp circulating ash 12 in low temperature pyrogenation chamber 14 mixes, high-temp circulating ash 12 is with part heat transferred pyrolyzing coal 10, pyrolytic reaction occurs in coal under 300 ~ 650 ℃ lesser temps, produce low temperature pyrogenation coal gas 7 and semicoke; Low temperature pyrogenation coal gas 7 enters the top of high temperature pyrolysis chamber 4 from the top of divider wall 5, the semicoke after the pyrolysis of coal and high-temp circulating ash together enter the bottom of high temperature pyrolysis chamber 4 from the bottom of divider wall 5;
Under the effect of the high temperature pyrolysis chamber fluidized gas 1 that is entered high temperature pyrolysis chamber 4 by bottom, high temperature pyrolysis chamber air distribution plate, semicoke after the pyrolysis of coal carries out high temperature fluidized the mixing in high temperature pyrolysis chamber 4 with high-temp circulating ash, high-temp circulating ash 12 continues more heat transferred semicokes, make semicoke under 600 ~ 950 ℃ comparatively high temps, continue to occur pyrolytic reaction, most of fugitive constituent in the semicoke is separated out, produce high temperature pyrolysis coal gas 6 and the very low semicoke of volatile content.
Bottom macrobead material 2 in the semicoke that this high temperature pyrolysis chamber produces and small part high-temp circulating ash enter the emulsion zone bottom of circular fluid bed from the bottom discharge nozzle of high temperature pyrolysis chamber 4, and the compound 3 that most of high-temp circulating ash and semicoke form enters the emulsion zone top of circular fluid bed through the returning charge valve of fluidized-bed combustion boiler from the top discharge nozzle of high temperature pyrolysis chamber 4; The at last after-flame utilization in circulating fluidized bed of semicoke after the pyrolysis of high temperature pyrolysis chamber.
High temperature pyrolysis coal gas 6 in these high temperature pyrolysis chamber 4 interior generations mixes at high temperature pyrolysis chamber 4 internal upper parts with the aforementioned low temperature pyrogenation coal gas 7 that enters high temperature pyrolysis chamber 4 internal upper parts, becomes temperature warm solution coal gas 8 in 450 ~ 850 ℃; In warm solution coal gas 8 enter pyrolysis gas waste-heat recovery device and pyrolyzing coal 10 heat exchange, behind the sensible heat transfer coal supply, the pyrolysis coal gas that this pyrolysis reactor produces enters the follow-up system such as pyrolysis gas purifying processing device and utilizes for collecting; The tar that gas cleaning device is collected also carries out the secondary pyrolysis in the high temperature pyrolysis chamber that turns back to capable of circulation.
Circulating gas after low temperature pyrogenation of the present invention chamber fluidized gas 15 and high temperature pyrolysis chamber fluidized gas 1 can purify for the coal gas process of steam or the generation of this pyrolysis reactor; In low temperature pyrogenation chamber 14, flow by control low temperature pyrogenation chamber fluidized gas 15, can control the fluidizing gas velocity in the low temperature pyrogenation chamber 14, change high-temp circulating ash 12 and in low temperature pyrogenation chamber 14, enter storage and the residence time of the circulating ash of upper space, thereby the temperature in the control low temperature pyrogenation chamber 14 and the mixed heat transfer intensity of pyrolyzing coal 10 and high-temp circulating ash 12, and then the reaction conditions of control low-temperature pyrolysis of coal, make it can adapt to Coal rank, the pyrolysis coal gas that produces contains more methane and light hydrocarbons etc., to improve heat value and quality; Usually the fluidization gas of this chamber is larger, and the circulating ash that enters upper space is more, and pyrolysis reaction temperature is higher.
Optionally, low temperature pyrogenation chamber fluidized gas and high temperature pyrolysis chamber fluidized gas are the inflammable gas of high combustion calorific value.
The present invention makes pyrolysis reactor the pyrolysis coal gas that produces and the pyrolyzing coal heat exchange that enters pyrolysis reactor by pyrolysis gas waste-heat recovery device 9, namely can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make the coal preheating, increase the pyrolysis ability of reactor; Pyrolysis gas waste-heat recovery device 9 can adopt multistage moving bed, make coal and pyrolysis gas countercurrent flow on the moving-bed, tar and the grit in the pyrolysis gas can be adsorbed and filter in the coal seam simultaneously, rough purification coal gas, recovery circulating ash, and make tar again enter repeatedly pyrolysis of pyrolysis reactor with coal, to improve the productive rate of pyrolysis gas, reduce the productive rate of tar.
The present invention can pass through to add the sweetening agents such as Wingdale in pyrolyzing coal, but not only desulfurization (under the reducing atmosphere) also has the effect of catalyse pyrolysis tar, can improve the productive rate of pyrolysis gas.
The present invention has following advantage:
1, the circulating ash heat transferred coal with circular fluid bed comes pyrolysis, adopts the mode heat-transfer capability of fluidized-bed to be better than the modes such as mix and blend heating, and exchange capability of heat is strong, and equipment and system are simple.Pyrolysis gas recirculation after the rough purification can improve the calorific value of pyrolysis gas as pyrolysis chamber's fluidizing agent, and this is very important for the lower low-rank coal of fugitive constituent calorific value;
2, the technique that adopts circulating ash to heat pyrolysis of coal is different from the pyrolysis oven of independent operating, because pyrolysis heat is from the sensible heat of circulating ash and on-fuel semicoke or coal, the UTILIZATION OF VESIDUAL HEAT IN of pyrolytic process is on the not impact of cold gas efficiency of pyrolysis, thereby the heats such as pyrolysis gas that adopt the circulating ash pyrolysis to reclaim also can be directly used in therrmodynamic system, needn't consider heat is all reclaimed for pyrolysis system, the system design of waste heat recovery can be more simple;
3, with directly at high temperature pyrolysis of coal, the methane content in the pyrolysis gas is few, and hydrogen content rises, and this is unfavorable for the operation of internal combustion turbine.The present invention adopts the mode of fluidized-bed stepped heating, can make at first at low temperatures pyrolysis of coal, improves the content of methane, at high temperature realizes at last abundant pyrolysis again, improves factor of created gase.In addition, the tar light oil that the low thermophase pyrolysis of the present invention produces carries out the secondary pyrolysis by entering the high temperature pyrolysis district again, has improved factor of created gase, has reduced tar yield;
4, because pyrolytic process of the present invention can make whole high-temp circulating ash of circular fluid bed enter pyrolysis reactor, thereby can improve the heat-exchange capacity of pyrolytic reaction and react final temperature, be conducive to realize efficient, the fully pyrolysis of coal;
5, the bottom of the present invention by making the low temperature pyrogenation chamber is a little more than the bottom of high temperature pyrolysis chamber, with the main body that adopts the pyrolysis chamber all be the up big and down small pyramidal structure in cross section, fluidized gas flow that can be less, realize active fluidization heat exchange and the conveying of coal, semicoke and circulating ash, thereby reduced energy consumption and thermosteresis that fluidized gas is brought;
6, the present invention makes pyrolysis coal gas and pyrolyzing coal heat exchange by the pyrolysis gas waste-heat recovery device, namely can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make the coal preheating, increases the pyrolysis ability of reactor; But the pyrolysis gas waste-heat recovery device is rough purification coal gas, recovery circulating ash also, and makes tar again enter repeatedly pyrolysis of pyrolysis reactor with coal, to improve the productive rate of pyrolysis gas, reduces the productive rate of tar;
7, the present invention can realize the secondary pyrolysis of tar light oil in the low temperature pyrogenation coal gas by low temperature pyrogenation coal gas is mixed with high temperature pyrolysis coal gas, increases the output of pyrolysis coal gas, reduces tar content; Mixed middle temperature gas temperature decreases than the pyrolysis final temperature of pyrolysis of coal reactor simultaneously, can reduce capacity and the resistance to flow of pyrolysis gas waste-heat recovery device, reduces the equipment and materials cost, improves the reliability of equipment.
Description of drawings
Fig. 1 is the synoptic diagram of fluidized bed classification pyrolysis of coal reactor of the present invention.
The accompanying drawing sign
1, high temperature pyrolysis chamber fluidized gas; 2, bottom macrobead material; 3, compound; 4, high temperature pyrolysis chamber; 5, divider wall; 6, high temperature pyrolysis coal gas; 7, low temperature pyrogenation coal gas; 8, warm solution coal gas in; 9, pyrolysis gas waste-heat recovery device; 10, pyrolyzing coal; 11, defeated device for coal; 12, high-temp circulating ash; 13, ash conveying device; 14, low temperature pyrogenation chamber; 15, low temperature pyrogenation chamber fluidized gas
Embodiment
Below be a most preferred embodiment of the present invention, it is only as explanation of the invention rather than restriction.
A kind of fluidized-bed reactor for pyrolysis of coal comprises pyrolysis chamber, divider wall 5, pyrolysis gas waste-heat recovery device 9, defeated device for coal 11, the outlet of macrobead material, high temperature pyrolysis chamber sulfuration gas entrance, compound outlet, the ash conveying device 13 that is made of low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4.
Wherein, separate by divider wall 5 low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4, low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 are connected in the upper and lower of divider wall 5 respectively, the height of divider wall 5 is higher than the emulsion zone height of two pyrolysis chambers, and the bottom air distribution plate of low temperature pyrogenation chamber 14 is a little more than the bottom air distribution plate of high temperature pyrolysis chamber 4.Wherein the bottom air distribution plate of low temperature pyrogenation chamber is used for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of high temperature pyrolysis chamber is used for the air inlet of high temperature pyrolysis chamber fluidized gas.
Defeated device for coal 11 and pyrolysis gas waste-heat recovery device are arranged in the top in the fluidized bed coal pyrolysis reactor pyrolysis chamber, and the separation shutoff by the pyrolyzing coal 10 that transports on it, top and the pyrolysis gas waste-heat recovery device 9 of low temperature pyrogenation chamber 14 are not directly linked, and 4 tops, high temperature pyrolysis chamber are connected with the pyrolysis gas waste-heat recovery device 9 of the section's of being located thereon outlet.
The main body of low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 all is the up big and down small taper in cross section, low temperature pyrogenation chamber 14 is connected with the ash inlet tube of high-temp circulating ash 12 at bed of material emulsion zone, this ash inlet tube is provided with ash conveying device 13, this ash conveying device can play the isolating seal effect, avoids the air-flow of low temperature pyrogenation chamber 14 to move back to ash inlet tube.
The high temperature pyrolysis chamber arranges the compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the less pyrolysis product semicoke of most of high-temp circulating ash and particle diameter, be provided with the compound outlet in bed of material emulsion zone bottom, be used for the discharging of the compound of the larger pyrolysis product semicoke of small part high-temp circulating ash and particle diameter.The process of utilizing said apparatus to carry out pyrolysis of coal comprises:
Pyrolyzing coal 10 is successively through entering low temperature pyrogenation chamber 14 behind pyrolysis gas waste-heat recovery device 9 and the defeated device for coal 11; High-temp circulating ash 12 from circular fluid bed enters low temperature pyrogenation chamber 14 via ash conveying device 13;
Under the effect of the low temperature pyrogenation chamber fluidized gas 15 that is entered low temperature pyrogenation chamber 14 by bottom, low temperature pyrogenation chamber air distribution plate, pyrolyzing coal 10 carries out the low temperature fluidisation with high-temp circulating ash 12 in low temperature pyrogenation chamber 14 mixes, high-temp circulating ash 12 is with part heat transferred pyrolyzing coal 10, pyrolytic reaction occurs in coal under 300 ~ 650 ℃ lesser temps, produce low temperature pyrogenation coal gas 7 and semicoke; Low temperature pyrogenation coal gas 7 enters the top of high temperature pyrolysis chamber 4 from the top of divider wall 5, the semicoke after the pyrolysis of coal and high-temp circulating ash together enter the bottom of high temperature pyrolysis chamber 4 from the bottom of divider wall 5;
Under the effect of the high temperature pyrolysis chamber fluidized gas 1 that is entered high temperature pyrolysis chamber 4 by bottom, high temperature pyrolysis chamber air distribution plate, semicoke after the pyrolysis of coal carries out high temperature fluidized the mixing in high temperature pyrolysis chamber 4 with high-temp circulating ash, high-temp circulating ash 12 continues more heat transferred semicokes, make semicoke under 600 ~ 950 ℃ comparatively high temps, continue to occur pyrolytic reaction, most of fugitive constituent in the semicoke is separated out, produce high temperature pyrolysis coal gas 6 and the very low semicoke of volatile content;
Bottom macrobead material 2 in the semicoke that this high temperature pyrolysis chamber produces and small part high-temp circulating ash enter the emulsion zone bottom of circular fluid bed from the bottom discharge nozzle of high temperature pyrolysis chamber 4, and the compound 3 that most of high-temp circulating ash and semicoke form enters the emulsion zone top of circular fluid bed through the returning charge valve of fluidized-bed combustion boiler from the top discharge nozzle of high temperature pyrolysis chamber 4; The at last after-flame utilization in circulating fluidized bed of semicoke after the pyrolysis of high temperature pyrolysis chamber;
High temperature pyrolysis coal gas 6 in these high temperature pyrolysis chamber 4 interior generations mixes at high temperature pyrolysis chamber 4 internal upper parts with the aforementioned low temperature pyrogenation coal gas 7 that enters high temperature pyrolysis chamber 4 internal upper parts, becomes temperature warm solution coal gas 8 in 450 ~ 850 ℃; In warm solution coal gas 8 enter pyrolysis gas waste-heat recovery device and pyrolyzing coal 10 heat exchange, behind the sensible heat transfer coal supply, the pyrolysis coal gas that this pyrolysis reactor produces enters the follow-up system such as pyrolysis coal gas purifying processing device and utilizes for collecting; The tar that gas cleaning device is collected also carries out the secondary pyrolysis in the high temperature pyrolysis chamber that turns back to capable of circulation.
Circulating gas after low temperature pyrogenation of the present invention chamber fluidized gas 15 and high temperature pyrolysis chamber fluidized gas 1 can purify for the coal gas process that steam, Sweet natural gas or this pyrolysis reactor produce; In low temperature pyrogenation chamber 14, flow by control low temperature pyrogenation chamber fluidized gas 15, can control the fluidizing gas velocity in the low temperature pyrogenation chamber 14, change high-temp circulating ash 12 and in low temperature pyrogenation chamber 14, enter storage and the residence time of the circulating ash of upper space, thereby the temperature in the control low temperature pyrogenation chamber 14 and the mixed heat transfer intensity of pyrolyzing coal 10 and high-temp circulating ash 12, and then the reaction conditions of control low-temperature pyrolysis of coal, make it can adapt to Coal rank, make the pyrolysis coal gas of generation contain more methane and light hydrocarbons etc., to improve heat value and quality; Usually the fluidization gas of this chamber is larger, and the circulating ash that enters upper space is more, and pyrolysis reaction temperature is higher.
The bottom air distribution plate of low temperature pyrogenation chamber 14 is a little more than the bottom air distribution plate of high temperature pyrolysis chamber 4, can guarantee that semicoke and circulating ash that low temperature pyrogenation chamber 14 is produced are delivered into high temperature pyrolysis chamber 4, thereby reduce energy consumption and thermosteresis that fluidized gas is brought.
The main body of low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 all is the up big and down small taper in cross section, can be under less fluidized gas flow, the air-flow velocity that ensures the bottom, pyrolysis chamber is higher, make the coal of greater particle size and semicoke in the abundant fluidisation in bottom, pyrolysis chamber, can ensure simultaneously that the air-flow velocity of separating top, hot cell reduces gradually, strengthen grain fluidized internal recycle amount, increase coal, semicoke and the high temperature circulation ash particle of small particle size in the emulsion zone residence time, be beneficial to abundant heat exchange and pyrolysis; By the discharge time of (the material valve on the discharge nozzle of bottom) control bottom macrobead material 2, can control the pyrolysis time of macrobead material.
The present invention makes pyrolysis reactor the pyrolysis coal gas that produces and the pyrolyzing coal heat exchange that enters pyrolysis reactor by pyrolysis gas waste-heat recovery device 9, namely can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make the coal preheating, increase the pyrolysis ability of reactor; Pyrolysis gas waste-heat recovery device 9 can adopt multistage moving bed, make coal and pyrolysis gas countercurrent flow on the moving-bed, tar and the grit in the pyrolysis gas can be adsorbed and filter in the coal seam simultaneously, rough purification coal gas, recovery circulating ash, and make tar again enter repeatedly pyrolysis of pyrolysis reactor with coal, to improve the productive rate of pyrolysis gas, reduce the productive rate of tar.
The present invention can pass through to add the sweetening agents such as Wingdale in pyrolyzing coal, but not only desulfurization (under the reducing atmosphere) also has the effect of catalyse pyrolysis tar, can improve the productive rate of pyrolysis gas.
Claims (11)
1. a fluidized bed classification pyrolysis of coal reactor is characterized in that, described reactor comprises pyrolysis chamber, divider wall, defeated device for coal, the outlet of macrobead material, compound outlet; Described pyrolysis chamber comprises low temperature pyrogenation chamber and high temperature pyrolysis chamber;
Separate by described divider wall described low temperature pyrogenation chamber and described high temperature pyrolysis chamber, and described low temperature pyrogenation chamber and described high temperature pyrolysis chamber are connected in the upper and lower of described divider wall respectively; The bottom air distribution plate of described low temperature pyrogenation chamber is used for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of described high temperature pyrolysis chamber is used for the air inlet of high temperature pyrolysis chamber fluidized gas;
The main body of described low temperature pyrogenation chamber and described high temperature pyrolysis chamber is the up big and down small taper in cross section, described low temperature pyrogenation chamber is connected with the ash inlet tube of high-temp circulating ash at bed of material emulsion zone, described high temperature pyrolysis chamber arranges the compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the less pyrolysis product semicoke of most of high-temp circulating ash and particle diameter, be provided with the compound outlet in bed of material emulsion zone bottom, be used for the discharging of the compound of the larger pyrolysis product semicoke of small part high-temp circulating ash and particle diameter.
2. reactor according to claim 1 is characterized in that, the height of described divider wall is higher than the emulsion zone height of described low temperature pyrogenation chamber and described high temperature pyrolysis chamber.
3. reactor according to claim 1 is characterized in that, the bottom air distribution plate of described low temperature pyrogenation chamber is higher than the bottom air distribution plate of described high temperature pyrolysis chamber.
4. reactor according to claim 1, it is characterized in that, described defeated device for coal is positioned at the top of fluidized bed coal pyrolysis reactor pyrolysis chamber, and the separation shutoff by the pyrolyzing coal that transports on it, and the top of low temperature pyrogenation chamber and pyrolysis gas waste-heat recovery device are not directly linked.
5. reactor according to claim 1 is characterized in that, described reactor also comprises the pyrolysis gas waste-heat recovery device, and described pyrolysis gas waste-heat recovery device is positioned at top, high temperature pyrolysis chamber, and is connected with the top of described high temperature pyrolysis chamber.
6. reactor according to claim 1 is characterized in that, described ash inlet tube place is provided with ash conveying device, is used for avoiding the air-flow of low temperature pyrogenation chamber to move back to ash inlet tube.
7. the method for utilizing the arbitrary described fluidized bed classification pyrolysis of coal reactor of claim 1～6 to carry out pyrolysis of coal comprises:
Pyrolyzing coal enters the low temperature pyrogenation chamber behind pyrolysis gas waste-heat recovery device and defeated device for coal; High-temp circulating ash from circular fluid bed enters the low temperature pyrogenation chamber via ash conveying device;
Described pyrolyzing coal mixes in the indoor low temperature fluidisation of carrying out of low temperature pyrogenation under the effect of the low temperature pyrogenation chamber fluidized gas that is entered the low temperature pyrogenation chamber by bottom, low temperature pyrogenation chamber air distribution plate with described high-temp circulating ash, high-temp circulating ash is with part heat transferred pyrolyzing coal, pyrolytic reaction occurs in pyrolyzing coal under 350 ~ 650 ℃ lesser temps, produce low temperature pyrogenation coal gas and semicoke; Described low temperature pyrogenation coal gas enters the top of high temperature pyrolysis chamber from the top of divider wall, the semicoke after the pyrolysis of coal and high-temp circulating ash together enter the bottom of high temperature pyrolysis chamber from the bottom of divider wall;
Semicoke after the described pyrolysis of coal and described high-temp circulating ash enter at bottom, high temperature pyrolysis chamber air distribution plate under the effect of high temperature pyrolysis chamber fluidized gas of high temperature pyrolysis chamber, carry out high temperature fluidized mixing in that high temperature pyrolysis is indoor, described high-temp circulating ash is with the heat transferred semicoke, make semicoke under 600 ~ 950 ℃ comparatively high temps, pyrolytic reaction occur, most of fugitive constituent in the semicoke is separated out, produce high temperature pyrolysis coal gas and the very low semicoke of volatile content;
Bottom macrobead material in the semicoke that described high temperature pyrolysis chamber produces and small part high-temp circulating ash enter the emulsion zone bottom of circular fluid bed from the bottom discharge nozzle of high temperature pyrolysis chamber, and the compound that most of high-temp circulating ash and semicoke form enters the emulsion zone top of circular fluid bed through the returning charge valve of circular fluid bed from the top discharge nozzle of high temperature pyrolysis chamber; The at last after-flame utilization in circular fluid bed of semicoke after the pyrolysis of high temperature pyrolysis chamber;
The high temperature pyrolysis coal gas of the indoor generation of described high temperature pyrolysis mixes on the indoor top of high temperature pyrolysis with the described low temperature pyrogenation coal gas that enters the indoor top of high temperature pyrolysis, becomes temperature warm solution coal gas in 450 ~ 850 ℃; Warm solution coal gas enters pyrolysis gas waste-heat recovery device and pyrolyzing coal heat exchange in described, and behind the heat transferred coal, the pyrolysis coal gas that this pyrolysis reactor produces enters pyrolysis coal gas purifying processing device and utilizes for collecting.
8. method according to claim 7 is characterized in that, the tar circulation that described pyrolyzing coal air purifying apparatus is collected turns back to the high temperature pyrolysis chamber and carries out the secondary pyrolysis.
9. method according to claim 7 is characterized in that, described method also is included in and adds sweetening agent in the pyrolyzing coal.
10. method according to claim 7, it is characterized in that, described method also is included in the low temperature fluid mapper process, flow by control low temperature pyrogenation chamber fluidized gas is controlled the indoor fluidizing gas velocity of low temperature pyrogenation, and then change high-temp circulating ash in indoor storage and the residence time that enters the circulating ash of upper space of low temperature pyrogenation, thereby control the indoor temperature of low temperature pyrogenation and the mixed heat transfer intensity of pyrolyzing coal and high-temp circulating ash.
11. method according to claim 7 is characterized in that, described low temperature pyrogenation chamber fluidized gas and high temperature pyrolysis chamber fluidized gas are inflammable gas.
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