CN103031135B - 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 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.Some pyrolysis are exactly to utilize the heat of coal combustion that the fugitive constituent in coal is separated out, just to directly obtaining coke or semicoke; Compare coal and coke, the fugitive constituent in coal has higher utility value mostly.Taking coal derived energy chemical as main pyrolytic process, mainly for producing tar and Hydrogenation oil fuel, the pyrolysis gas that pyrolysis produces conventionally directly burns to be needed 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, byproduct pyrolysis gas directly burns for producing steam generating; Another pyrolysis of coal is that to improve generating efficiency be object, pyrolytic process is to produce pyrolysis gas as main, the semicoke producing except pyrolysis produces steam-electric power by burning, and the pyrolysis gas of generation also can improve overall coal power generation efficiency by gas combustion-gas vapor combined cycle.
Pyrolysis of coal is utilization object mainly with the higher low-disintegration coal of fugitive constituent greatly, low-quality pit ash is large, ash fusion point is low, semicoke calorific value after pyrolysis is low, if the high temperature semicoke after pyrolysis is for the burning of pulverized coal firing boiler, not only need the cooling of high temperature semicoke, increase 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 supporting fly-ash separator of coal-powder boiler, the capacity of grey transport process system also need greatly to improve.Thereby for will be by the system of the direct combustion power generation of pyrolysis product semicoke, should not adopt the special pyrolysis of independent pyrolysis oven, but pyrolysis system and firing system should be combined.
No matter the heat of pyrolysis of coal is still provided using solid as thermal barrier using gas as thermal barrier, 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 to be also difficult for.Because the mutual heat transfer condition of different media in fluidized-bed layer is splendid, thereby utilize fluid bed heat analytical system and equipment comparatively simple, better results.
For the system that pyrolysis product semicoke directly will be burnt, pyrolysis heat can reach 800 DEG C of above high-temp circulating ash by circular fluid bed temperature to be provided, high temperature semicoke after pyrolysis directly enters fluidized-bed combustion boiler burning with circulating ash, the technique that reduces semicoke high temperature conveying and UTILIZATION OF VESIDUAL HEAT IN, equipment and flow process are comparatively simple.
Tradition fluidized-bed pyrolytic process of coal is all that to produce tar be main purpose, obtains good coal utilization comprehensive benefit by producing more high-quality tar.Such processing requirement produces low temperature tar light oil, thereby pyrolysis temperature can not be too high, is conventionally controlled at below 600 DEG C.If utilize the circulating ash of circular fluid bed as thermal barrier, carry out under suitable low temperature in order to control pyrolytic reaction in fluidized bed pyrolysis reactor, this pyrolytic process only need to be controlled part high-temp circulating ash is entered to fluidized-bed reactor, and other circulating ash is directly returned to fluidized-bed combustion boiler.For most coals, if make full use of the fugitive constituent of coal, need at higher temperature, just can complete the abundant pyrolysis of coal, produce more a high proportion of pyrolysis gas simultaneously.But in the pyrolysis gas of the direct high temperature pyrolysis of coal, methane content is few, and hydrogen richness is many, this pyrolysis coal gas is unfavorable for that gas turbine group is in economic and safe operating mode operation.
Summary of the invention
The object of the invention is by adopt fluidized-bed to carry out coal grading pyrolytic process, can ensure produce that how suitable gas turbine combustion needs compared with the pyrolysis gas of good quality, 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 first in the indoor pyrolysis of carrying out under low temperature of first step fluidized bed pyrolysis, and then enters that next stage fluidized bed pyrolysis is indoor carries out pyrolysis under comparatively high temps.The circulating ash that pyrolysis heat is exported by circulating fluidized bed boiler separator provides, 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 Liang Ge pyrolysis chamber.
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 the semicoke and the circulating ash that under lower fluidized gas flow, make low temperature pyrogenation chamber 14 produce 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 for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of described high temperature pyrolysis chamber is 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 is all the up big and down small taper in cross section, can be under less fluidized gas flow, the air-flow velocity that ensures bottom, pyrolysis chamber is higher, make the coal of greater particle size and semicoke in the abundant fluidisation in bottom, pyrolysis chamber, can ensure that the air-flow velocity of separating top, hot cell reduces gradually simultaneously, 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; Control the discharge time of bottom macrobead material 2 by (the material valve on the discharge nozzle of bottom), 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 fluidized bed coal pyrolysis reactor pyrolysis chamber, and by the separation shutoff of 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 connected.
Optionally, described device also comprises 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 is all 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 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 compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the pyrolysis product semicoke that most of high-temp circulating ash and particle diameter are less, be provided with compound outlet in bed of material emulsion zone bottom, for the discharging of the compound of small part high-temp circulating ash and the larger pyrolysis product semicoke of particle diameter.
The process of utilizing said apparatus to carry out pyrolysis of coal comprises:
Pyrolyzing coal 10 successively enters low temperature pyrogenation chamber 14 after pyrolysis gas waste-heat recovery device 9 and 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.
Entered by bottom, low temperature pyrogenation chamber air distribution plate under the effect of low temperature pyrogenation chamber fluidized gas 15 of low temperature pyrogenation chamber 14, pyrolyzing coal 10 carries out low temperature fluidisation in low temperature pyrogenation chamber 14 to be mixed with high-temp circulating ash 12, part heat is passed to pyrolyzing coal 10 by high-temp circulating ash 12, coal issues raw pyrolytic reaction at the lesser temps of 300 ~ 650 DEG C, produces 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 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;
Entered by bottom, high temperature pyrolysis chamber air distribution plate under the effect of high temperature pyrolysis chamber fluidized gas 1 of high temperature pyrolysis chamber 4, semicoke after pyrolysis of coal carries out high temperature fluidized mixing in high temperature pyrolysis chamber 4 with high-temp circulating ash, high-temp circulating ash 12 continues more heats to pass to semicoke, make semicoke under the comparatively high temps of 600 ~ 950 DEG C, continue to occur pyrolytic reaction, most of fugitive constituent in 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, the compound 3 of most of high-temp circulating ash and semicoke composition 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 finally 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 DEG C; In warm solution coal gas 8 enter pyrolysis gas waste-heat recovery device and pyrolyzing coal 10 heat exchange, by after sensible heat transfer coal supply, the pyrolysis coal gas that this pyrolysis reactor produces enters the follow-up systems such as pyrolysis gas purifying processing device and utilizes for collecting; The tar that gas cleaning device is collected also carries out secondary pyrolysis in the high temperature pyrolysis chamber that turns back to capable of circulation.
Low temperature pyrogenation of the present invention chamber fluidized gas 15 and high temperature pyrolysis chamber fluidized gas 1 can be the circulating gas of the coal gas that produces of steam or this pyrolysis reactor after purifying; In low temperature pyrogenation chamber 14, by controlling the flow of low temperature pyrogenation chamber fluidized gas 15, can control the fluidizing gas velocity in 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 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 producing contains more methane and light hydrocarbons etc., to improve calorific value and the quality of coal gas; Conventionally 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 pyrolysis coal gas that the present invention produces pyrolysis reactor by pyrolysis gas waste-heat recovery device 9 and the pyrolyzing coal heat exchange that enters pyrolysis reactor, can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make 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 moving-bed, tar and the grit in pyrolysis gas can be adsorbed and filter in coal seam simultaneously, rough purification coal gas, recovery circulating ash, and make tar again enter pyrolysis reactor pyrolysis repeatedly with coal, to improve the productive rate of pyrolysis gas, reduce the productive rate of tar.
The present invention can be by adding the sweetening agents such as Wingdale in pyrolyzing coal, not only can desulfurization (under reducing atmosphere) also has the effect of catalyse pyrolysis tar, can improve the productive rate of pyrolysis gas.
Tool of the present invention has the following advantages:
1, the circulating ash heat of circular fluid bed is transmitted to coal supply and carry out pyrolysis, adopt the mode heat-transfer capability of fluidized-bed to be better than the modes such as mix and blend heating, exchange capability of heat is strong, and equipment and system are simple.Pyrolysis gas recirculation after rough purification can improve the calorific value of pyrolysis gas as pyrolysis chamber's fluidizing agent, this is very important for the lower low-rank coal of fugitive constituent calorific value;
2, adopt the technique of circulating ash heating pyrolysis of coal to be 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 does not affect the cold gas efficiency of pyrolysis, thereby adopt the heats such as pyrolysis gas that circulating ash pyrolysis reclaims also can be directly used in therrmodynamic system, needn't consider heat all to reclaim for pyrolysis system, the system design of waste heat recovery can be more simple;
3, by directly at high temperature pyrolysis of coal, the methane content in 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 coal pyrolysis first at low temperatures, improves the content of methane, finally at high temperature realizes 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 secondary pyrolysis by entering high temperature pyrolysis district again, has improved factor of created gase, has reduced tar yield;
4, enter pyrolysis reactor because pyrolytic process of the present invention can make whole high-temp circulating ash of circular fluid bed, thereby can improve heat-exchange capacity and the reaction final temperature of pyrolytic reaction, be conducive to realize efficient, the fully pyrolysis of coal;
5, the present invention is by making the bottom of low temperature pyrogenation chamber a little more than the bottom of high temperature pyrolysis chamber, be all the up big and down small pyramidal structure in cross section with adopting the main body of pyrolysis chamber, 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 pyrolysis gas waste-heat recovery device, can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make coal preheating, increases the pyrolysis ability of reactor; Pyrolysis gas waste-heat recovery device also can rough purification coal gas, reclaim circulating ash, and make tar again enter pyrolysis reactor pyrolysis repeatedly with coal, to improve the productive rate of pyrolysis gas, reduces the productive rate of tar;
7, the present invention, by low temperature pyrogenation coal gas is mixed with high temperature pyrolysis coal gas, can realize the secondary pyrolysis of tar light oil in low temperature pyrogenation 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 equipment and materials cost, improves the reliability of equipment.
Brief description of the drawings
Fig. 1 is the schematic diagram of fluidized bed classification pyrolysis of coal reactor of the present invention.
Accompanying drawing mark
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
Be below a most preferred embodiment of the present invention, it is only as explanation of the invention instead of restriction.
A kind of fluidized-bed reactor for pyrolysis of coal comprises the 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 are made up 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 Liang Ge pyrolysis chamber, 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 for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of high temperature pyrolysis chamber is 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 fluidized bed coal pyrolysis reactor pyrolysis chamber, and by the separation shutoff of 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 connected, and 4 tops, high temperature pyrolysis chamber are connected with the pyrolysis gas waste-heat recovery device 9 of the portion's of being located thereon outlet.
The main body of low temperature pyrogenation chamber 14 and high temperature pyrolysis chamber 4 is all 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 isolating seal effect, avoids the air-flow of low temperature pyrogenation chamber 14 to move back to ash inlet tube.
High temperature pyrolysis chamber arranges compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the pyrolysis product semicoke that most of high-temp circulating ash and particle diameter are less, be provided with compound outlet in bed of material emulsion zone bottom, for the discharging of the compound of small part high-temp circulating ash and the larger pyrolysis product semicoke of particle diameter.The process of utilizing said apparatus to carry out pyrolysis of coal comprises:
Pyrolyzing coal 10 successively enters low temperature pyrogenation chamber 14 after pyrolysis gas waste-heat recovery device 9 and 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;
Entered by bottom, low temperature pyrogenation chamber air distribution plate under the effect of low temperature pyrogenation chamber fluidized gas 15 of low temperature pyrogenation chamber 14, pyrolyzing coal 10 carries out low temperature fluidisation in low temperature pyrogenation chamber 14 to be mixed with high-temp circulating ash 12, part heat is passed to pyrolyzing coal 10 by high-temp circulating ash 12, coal issues raw pyrolytic reaction at the lesser temps of 300 ~ 650 DEG C, produces 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 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;
Entered by bottom, high temperature pyrolysis chamber air distribution plate under the effect of high temperature pyrolysis chamber fluidized gas 1 of high temperature pyrolysis chamber 4, semicoke after pyrolysis of coal carries out high temperature fluidized mixing in high temperature pyrolysis chamber 4 with high-temp circulating ash, high-temp circulating ash 12 continues more heats to pass to semicoke, make semicoke under the comparatively high temps of 600 ~ 950 DEG C, continue to occur pyrolytic reaction, most of fugitive constituent in 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, the compound 3 of most of high-temp circulating ash and semicoke composition 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 finally 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 DEG C; In warm solution coal gas 8 enter pyrolysis gas waste-heat recovery device and pyrolyzing coal 10 heat exchange, by after sensible heat transfer coal supply, the pyrolysis coal gas that this pyrolysis reactor produces enters the follow-up systems such as pyrolysis coal gas purifying processing device and utilizes for collecting; The tar that gas cleaning device is collected also carries out secondary pyrolysis in the high temperature pyrolysis chamber that turns back to capable of circulation.
Low temperature pyrogenation of the present invention chamber fluidized gas 15 and high temperature pyrolysis chamber fluidized gas 1 can be the circulating gas of the coal gas that produces of steam, Sweet natural gas or this pyrolysis reactor after purifying; In low temperature pyrogenation chamber 14, by controlling the flow of low temperature pyrogenation chamber fluidized gas 15, can control the fluidizing gas velocity in 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 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 producing contain more methane and light hydrocarbons etc., to improve calorific value and the quality of coal gas; Conventionally 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 the semicoke and the circulating ash that under lower fluidized gas flow, make low temperature pyrogenation chamber 14 produce 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 is all the up big and down small taper in cross section, can be under less fluidized gas flow, the air-flow velocity that ensures bottom, pyrolysis chamber is higher, make the coal of greater particle size and semicoke in the abundant fluidisation in bottom, pyrolysis chamber, can ensure that the air-flow velocity of separating top, hot cell reduces gradually simultaneously, 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; Control the discharge time of bottom macrobead material 2 by (the material valve on the discharge nozzle of bottom), can control the pyrolysis time of macrobead material.
The pyrolysis coal gas that the present invention produces pyrolysis reactor by pyrolysis gas waste-heat recovery device 9 and the pyrolyzing coal heat exchange that enters pyrolysis reactor, can improve thermo-efficiency and the cold gas efficiency of pyrolysis reactor, also can make 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 moving-bed, tar and the grit in pyrolysis gas can be adsorbed and filter in coal seam simultaneously, rough purification coal gas, recovery circulating ash, and make tar again enter pyrolysis reactor pyrolysis repeatedly with coal, to improve the productive rate of pyrolysis gas, reduce the productive rate of tar.
The present invention can be by adding the sweetening agents such as Wingdale in pyrolyzing coal, not only can desulfurization (under 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 for the air inlet of low temperature pyrogenation chamber fluidized gas, and the bottom air distribution plate of described high temperature pyrolysis chamber is 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 compound outlet on bed of material emulsion zone top, be used for the discharging of the compound of the pyrolysis product semicoke that most of high-temp circulating ash and particle diameter are less, be provided with macrobead material outlet in bed of material emulsion zone bottom, for the discharging of the compound of small part high-temp circulating ash and the larger pyrolysis product semicoke of 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 classification pyrolysis of coal reactor pyrolysis chamber, and by the separation shutoff of the pyrolyzing coal that transports on it, the top of low temperature pyrogenation chamber and pyrolysis gas waste-heat recovery device is not directly connected.
5. reactor according to claim 1, is characterized in that, described reactor also comprises 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, moves back to ash inlet tube for the air-flow of avoiding low temperature pyrogenation chamber.
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, comprising:
Pyrolyzing coal enters low temperature pyrogenation chamber after pyrolysis gas waste-heat recovery device and defeated device for coal; High-temp circulating ash from circular fluid bed enters 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 low temperature pyrogenation chamber fluidized gas that is entered low temperature pyrogenation chamber by bottom, low temperature pyrogenation chamber air distribution plate with described high-temp circulating ash, part heat is passed to pyrolyzing coal by high-temp circulating ash, pyrolyzing coal issues raw pyrolytic reaction at the lesser temps of 350～650 DEG C, produces 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 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 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 high temperature pyrolysis is indoor, described high-temp circulating ash transfers heat to semicoke, make semicoke issue raw pyrolytic reaction at the comparatively high temps of 600～950 DEG C, most of fugitive constituent in 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, the compound of most of high-temp circulating ash and semicoke composition 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 finally 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 with described in enter the indoor top of high temperature pyrolysis low temperature pyrogenation coal gas mix on the indoor top of high temperature pyrolysis, become temperature warm solution coal gas in 450～850 DEG C; In described, warm solution coal gas enters pyrolysis gas waste-heat recovery device and pyrolyzing coal heat exchange, transfers heat to after coal, and 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 high temperature pyrolysis chamber and carries out secondary pyrolysis.
9. method according to claim 7, is characterized in that, described method is also included in and in pyrolyzing coal, adds sweetening agent.
10. method according to claim 7, it is characterized in that, described method is also included in low temperature fluid mapper process, control the indoor fluidizing gas velocity of low temperature pyrogenation by the flow of controlling low temperature pyrogenation chamber fluidized gas, and then change high-temp circulating ash in storage and the residence time of the indoor circulating ash that enters 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. methods 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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